CN117247791A - Cracking device and cracking method - Google Patents
Cracking device and cracking method Download PDFInfo
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- CN117247791A CN117247791A CN202210657296.9A CN202210657296A CN117247791A CN 117247791 A CN117247791 A CN 117247791A CN 202210657296 A CN202210657296 A CN 202210657296A CN 117247791 A CN117247791 A CN 117247791A
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- 238000000034 method Methods 0.000 title claims abstract description 31
- 238000005336 cracking Methods 0.000 title claims description 36
- 238000006243 chemical reaction Methods 0.000 claims abstract description 152
- 239000003054 catalyst Substances 0.000 claims abstract description 118
- 238000000197 pyrolysis Methods 0.000 claims abstract description 43
- 230000008929 regeneration Effects 0.000 claims description 37
- 238000011069 regeneration method Methods 0.000 claims description 37
- 238000005243 fluidization Methods 0.000 claims description 28
- 239000003795 chemical substances by application Substances 0.000 claims description 21
- 230000008569 process Effects 0.000 claims description 17
- 230000003197 catalytic effect Effects 0.000 claims description 10
- 238000009826 distribution Methods 0.000 claims description 6
- 238000004891 communication Methods 0.000 claims description 5
- 238000012546 transfer Methods 0.000 claims description 5
- 239000007787 solid Substances 0.000 abstract description 56
- 239000000571 coke Substances 0.000 abstract description 9
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 6
- 239000002994 raw material Substances 0.000 abstract description 6
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 230000007246 mechanism Effects 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 76
- 230000000694 effects Effects 0.000 description 66
- 239000007789 gas Substances 0.000 description 47
- 239000003502 gasoline Substances 0.000 description 14
- 239000002283 diesel fuel Substances 0.000 description 7
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 7
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 7
- 239000000295 fuel oil Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 238000004523 catalytic cracking Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 230000000630 rising effect Effects 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000003776 cleavage reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- -1 ethylene, propylene, butylene Chemical group 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000008041 oiling agent Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 238000010517 secondary reaction Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
- C10G11/182—Regeneration
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The embodiment of the application discloses a pyrolysis device and pyrolysis method, and the pyrolysis device includes: a first reactor in which a first reaction zone is formed; the second reactor, one end of the first reactor is located in the second reactor, there is a second reaction zone in the second reactor; the sleeve is sleeved at one end of the first reactor, which is positioned in the second reactor; an oil distributor disposed between the sleeve and the first reactor; and the catalyst distributor is arranged at the upper part of the sleeve. By the pyrolysis device, the reaction temperatures of the respective reaction zones are respectively controlled by the circulation amount of the regenerated catalyst/solid heat carrier entering the respective reaction zones, and the aim of independently controlling the reaction temperatures of the different reaction zones is fulfilled. The method realizes the zonal reaction of raw materials with different properties according to the respective reaction mechanism requirements, realizes the independent control of the temperatures of different reaction areas, can obviously reduce the yields of byproducts such as dry gas, coke and the like, and improves the yield and selectivity of the low-carbon olefin.
Description
Technical Field
The embodiment of the application relates to the technical field of petrochemical reactions, in particular to a cracking device and a cracking method.
Background
The cracking in petrochemical industry is to use catalyst or solid heat carrier to crack petroleum hydrocarbon at high temperature to produce low-carbon olefin such as ethylene, propylene, butylene, etc. and light aromatic hydrocarbon, and is a key technology for refining, converting and upgrading in oil refinery. Compared with catalytic cracking, the cracking adopts higher reaction temperature and larger catalyst-oil ratio, the reaction condition is more severe, the conventional catalytic cracking riser reactor cannot be simply used, and the design and optimization of a cracking method and a reaction device are always focuses of attention of all parties.
The Chinese petrochemical science institute (hereinafter referred to as Shikoku) develops a catalytic cracking (Deep Catalytic Cracking-DCC) process which takes heavy oil as a raw material and propylene as a main purpose, and is characterized in that a riser and dense-phase fluidized bed combined reactor technology is adopted, paraffin-based raw materials are adopted as a preference, a riser reactor adopts a higher reaction temperature, a dense-phase bed adopts a low-airspeed process condition, and the propylene yield is 15-22%. The DCC process has the problem that the temperatures of the two reaction zones (the riser is one-reaction and the dense-phase fluidized bed is two-reaction) cannot be controlled independently, and in order to ensure the reaction temperature of the two reactions, the heavy oil reaction temperature of the one-reaction riser is very high, so that the dry gas and coke yield are high.
Based on DCC process, dan Keyuan developed DCC-plus process with high propylene selectivity. The DCC-plus process has the added second riser (three-reaction) to dense-phase fluidized bed to replenish regenerated catalyst, and this can control the two-reaction temperature independently, lower the outlet temperature of the main riser and lower the dry gas and coke yield. The DCC-Plus process solves the problem that the temperature of the DCC secondary reaction zone cannot be independently controlled, but the high-activity catalyst returned by three-reaction cannot be uniformly distributed on the oversized cross section of the secondary dense-phase fluidized bed, so that the activity of the secondary catalyst is different, and the yield and the selectivity of olefin are affected.
Disclosure of Invention
The present invention aims to solve at least one of the technical problems existing in the prior art or related art.
To this end, a first aspect of the invention provides a pyrolysis apparatus.
In a second aspect the invention provides a method of cleavage.
In view of this, there is provided, according to a first aspect of an embodiment of the present application, a cracking apparatus, including:
a first reactor having a first reaction zone formed therein;
the second reactor, one end of the said first reactor locates at the inside of the said second reactor, there is a second reaction zone in the said second reactor;
the sleeve is sleeved at one end of the first reactor, which is positioned in the second reactor, and a gap is reserved between the outer wall of the sleeve and the second reactor;
an oil distributor is disposed between the sleeve and the first reactor.
In one possible embodiment, the finish dispenser comprises:
the distribution pipe is provided with a first through hole; wherein, oil agent distributor is a plurality of.
In one possible embodiment, the first reactor comprises: a fluidized bed reactor or riser reactor; the second reactor is a dense phase fluidized bed.
In one possible embodiment, the pyrolysis apparatus further comprises:
and the lifter is connected with one end of the first reactor, which is away from the second reactor.
In one possible embodiment, the pyrolysis apparatus further comprises:
the first fluidization ring is provided with a second through hole, and is arranged in the second reactor and positioned between the sleeve and the second reactor;
the second fluidization ring is provided with a third through hole, and the second fluidization ring is arranged at one end of the first reaction container, which is close to the second reactor;
and a steam supply device communicated with the first fluidization ring and the second fluidization ring.
In one possible embodiment, the pyrolysis apparatus further comprises:
the first feeding pipe is communicated with the first reactor;
the conveying pipe is connected to one end, far away from the first reactor, of the second reactor;
a stripping section through which the transfer tube passes;
a settler connected to the other end of the delivery pipe;
a separator disposed within the settler;
and the waiting inclined tube is communicated with the stripping part.
In one possible embodiment, the pyrolysis apparatus further comprises:
and the catalytic regeneration system is communicated with the waiting inclined tube.
In one possible embodiment, the pyrolysis apparatus further comprises:
and the first regeneration inclined pipe is communicated with the first reactor and the catalytic regeneration system.
In one possible embodiment, the pyrolysis apparatus further comprises:
and a catalyst distributor, wherein the catalyst distributor is arranged in the second reactor, and the output end of the catalyst distributor is arranged towards the sleeve.
In one possible embodiment, the pyrolysis apparatus further comprises:
a second regeneration chute, which is communicated with the catalyst distributor;
the second feeding pipe is communicated with the second reactor and is positioned between the catalyst distributor and the first reaction container; or (b)
A third reaction zone riser in communication with the catalyst distributor;
the third regeneration inclined tube is communicated with the third reaction zone lifting tube;
and the third feeding pipe is communicated with the third reaction zone lifting pipe.
According to a second aspect of embodiments of the present application, there is provided a pyrolysis apparatus for any one of the above technical solutions, the pyrolysis method includes:
the feed rate of the raw oil is controlled so that the residence time of the raw oil in the first reaction zone is 1s to 2s, and the residence time of the oil gas in the second reaction zone is 2s to 5s;
wherein the reaction temperature of the first reaction zone is 550 ℃ to 600 ℃, and the reaction temperature of the second reaction zone is 630 ℃ to 730 ℃.
Compared with the prior art, the invention at least comprises the following beneficial effects: the cracking device provided by the embodiment of the application comprises a first reactor, a second reactor, a sleeve and an oiling agent distributor, wherein in the use process, raw oil, a high-temperature high-activity catalyst and a solid heat carrier are conveyed into the first reactor, and a cracking reaction of heavy oil is carried out in a first reactor zone of the first reactor, so that a lower reaction severity scale can be adopted, the residence time is shorter, intermediate components such as liquefied gas, gasoline, diesel oil and the like are mainly generated, and the yield of dry gas and coke is controlled; the method comprises the steps that raw oil, a high-temperature high-activity catalyst and a solid heat carrier are subjected to a cracking reaction in a first reaction zone, then the high-temperature high-activity catalyst is changed into a low-temperature low-activity catalyst, the low-temperature low-activity catalyst and the solid heat carrier are conveyed into a second reactor through a first reactor, in the process, oil gas in materials fed into the second reactor through the first reactor can be primarily separated from the low-temperature low-activity catalyst and the low-temperature solid heat carrier through a sleeve and an oil agent distributor, the oil gas can be fed into the second reactor through the oil agent distributor, part of the low-temperature low-activity catalyst and the low-temperature solid heat carrier can be blocked by the oil agent distributor, and the oil gas entering the second reactor can be contacted and mixed with the high-temperature high-activity catalyst/the high-temperature solid heat carrier newly added into the second reactor to form a high-severity reaction zone for deep cracking of intermediate components such as C4, gasoline and diesel oil; the low-temperature low-activity catalyst and the low-temperature solid heat carrier which are preliminarily separated by the sleeve and the oil agent distributor can flow upwards from the inside of the sleeve, and part of the low-temperature low-activity catalyst flows upwards from the outside of the sleeve, so that at least part of the low-temperature low-activity catalyst cannot be mixed with the high-temperature high-activity catalyst newly fed into the second reactor, the reaction efficiency in the second reactor can be ensured, and the petrochemical reaction efficiency is improved.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the application. Also, like reference numerals are used to designate like parts throughout the figures. In the drawings:
FIG. 1 is a schematic block diagram of a pyrolysis apparatus according to one embodiment provided herein;
FIG. 2 is a schematic block diagram of a pyrolysis apparatus according to another embodiment provided herein.
The correspondence between the reference numerals and the component names in fig. 1 and 2 is:
1 riser, 2 first feed pipe, 3 first reactor, 4 second fluidization ring, 5 first fluidization ring, 6 sleeve, 7 oil distributor, 8 transfer pipe, 9 stripping section, 10 settler, 11 separator, 12 second reactor, 13 catalyst distributor, 14 third reaction zone riser, 15 third feed pipe, 16 waiting inclined pipe, 17 first regeneration inclined pipe, 18 third regeneration inclined pipe, 19 second regeneration inclined pipe, 20 second feed pipe.
Detailed Description
In order to better understand the technical solutions described above, the technical solutions of the embodiments of the present application are described in detail below through the accompanying drawings and the specific embodiments, and it should be understood that the embodiments of the present application and the specific features in the embodiments are detailed descriptions of the technical solutions of the embodiments of the present application, and not limit the technical solutions of the present application, and the embodiments of the present application and the technical features in the embodiments of the present application may be combined with each other without conflict.
As shown in fig. 1 and 2, in view of this, according to a first aspect of an embodiment of the present application, there is provided a pyrolysis apparatus, including: a first reactor 3, a first reaction zone being formed in the first reactor 3; a second reactor 12, one end of the first reactor 3 is positioned in the second reactor 12, and a second reaction zone is formed in the second reactor 12; the sleeve 6 is sleeved at one end of the first reactor 3 positioned in the second reactor 12, and a gap is reserved between the outer wall of the sleeve 6 and the second reactor 12; an oil distributor 7 is arranged between the sleeve 6 and the first reactor 3.
The cracking device provided by the embodiment of the application comprises a first reactor 3, a second reactor 12, a sleeve 6 and an oil agent distributor 7, wherein in the use process, raw oil, a high-temperature high-activity catalyst and a solid heat carrier are conveyed into the first reactor 3, and the cracking reaction of heavy oil is carried out in the first reactor 3 area of the first reactor 3, so that a lower reaction severity scale and a shorter residence time can be adopted, intermediate components such as liquefied gas, gasoline, diesel oil and the like are mainly generated, and the yield of dry gas and coke is controlled; the raw oil, the high-temperature high-activity catalyst and the solid heat carrier are subjected to cracking reaction in the first reaction zone, then the high-temperature high-activity catalyst is changed into a low-temperature low-activity catalyst, the low-temperature low-activity catalyst and the solid heat carrier are conveyed into the second reactor 12 through the first reactor 3, in the process, the sleeve 6 and the oil agent distributor 7 can perform primary separation on oil gas in materials fed into the second reactor 12 through the first reactor 3, the low-temperature low-activity catalyst and the low-temperature solid heat carrier, the oil gas can be fed into the second reactor 12 through the oil agent distributor 7, part of the low-temperature low-activity catalyst and the low-temperature solid heat carrier can be blocked by the oil agent distributor 7, and the oil gas entering into the second reactor 12 can be contacted and mixed with the high-temperature high-activity catalyst/the high-temperature solid heat carrier newly added into the second reactor to form a high-temperature reaction zone for deep cracking of C4, gasoline, diesel oil and other intermediate components; the low-temperature low-activity catalyst and the low-temperature solid heat carrier which are preliminarily separated by the sleeve 6 and the oil agent distributor 7 can flow upwards from the inside of the sleeve 6 under the action of the oil-gas thrust, and flow upwards from the outside of the sleeve 6, so that at least part of the low-temperature low-activity catalyst cannot be mixed with the high-temperature high-activity catalyst newly fed into the second reactor 12, the reaction efficiency in the second reactor 12 can be ensured, and the petrochemical reaction efficiency can be improved.
In one possible embodiment, the finish dispenser 7 comprises: a distribution pipe provided with a first through hole; wherein, the oil agent distributor 7 is a plurality of.
The oil agent distributor 7 comprises a distributing pipe, wherein a first through hole is formed in the distributing pipe, in the use process, as raw oil is continuously input into the first reactor 3, after the raw oil is subjected to cracking reaction in the first reaction zone to generate oil gas, a mixture of the oil gas, the low-temperature low-activity catalyst and the low-temperature solid heat carrier flows to the second reactor 12, in the process, the distributing pipe can block the low-temperature low-activity catalyst and the low-temperature solid heat carrier, and the oil gas can pass through the distributing pipe through the first through hole and be conveyed into the second reactor 12.
It will be appreciated that the number of the oil distributors 7 may be plural, and the apertures and/or the number of the first through holes of the oil distributors 7 may be different, so that the blocking efficiencies of the low-temperature low-activity catalyst and the low-temperature solid heat carrier by the oil distributors 7 may be different, and in the actual production process, the proper oil distributors 7 may be selected to be assembled, so as to realize adjustment of the preliminary separation efficiency of the low-temperature low-activity catalyst and the low-temperature solid heat carrier.
In a possible embodiment, the first reactor 3 comprises: a fluidized bed reactor or riser reactor; the second reactor 12 is a dense phase fluidized bed.
The cracker provided by the embodiment of the application adopts the subregion setting, and wherein first reaction zone adopts riser reactor or fluidized bed reactor + riser delivery segment for the pyrolysis reaction of heavy oil adopts lower reaction severity scale, and shorter dwell time mainly generates intermediate component such as liquefied gas, petrol and diesel oil, control dry gas and coke yield. The end of the first reaction zone is provided with an oil distributor 7 for distributing and primarily separating oil gas from the low-temperature low-activity catalyst/low-temperature solid heat carrier. A sleeve 6 is arranged between the tail end of the first reaction zone and the second reaction zone to form an annular fluidized bed, a part of low-temperature low-activity catalyst flows upwards from the inside of the sleeve 6, a part of low-temperature low-activity catalyst flows upwards from the outside of the sleeve 6, and the flow rate of the catalyst inside and outside the sleeve 6 can be regulated through the flow rate of fluidization steam outside the sleeve 6.
In one possible embodiment, the second reactor 12 is a dense fluid bed.
The second reaction zone adopts a dense-phase fluidized bed type, and the ascending oil gas and catalyst/solid heat carrier in the annular fluidized bed sleeve 6 are contacted and mixed with the high-temperature high-activity catalyst/high-temperature solid heat carrier to form a high-severity reaction zone for deep cracking of intermediate components such as C4, gasoline, diesel oil and the like.
As shown in fig. 1 and 2, in one possible embodiment, the pyrolysis apparatus further comprises: the riser 1 is connected to the end of the first reactor 3 facing away from the second reactor 12.
By the provision of the riser 1, the regenerated high temperature high activity catalyst and solid heat carrier can be conveniently transported into the first reactor 3.
In one possible embodiment, the pyrolysis apparatus further comprises: a first fluidization ring 5, wherein a second through hole is formed in the fluidization ring, and the first fluidization ring 5 is arranged in the second reactor and is positioned between the sleeve 6 and the second reactor; a second fluidization ring 4, wherein a third through hole is formed in the fluidization ring, and the second fluidization ring 4 is arranged at one end of the first reaction container close to the second reactor 12; steam supply means communicating with the first fluidization ring 5 and the second fluidization ring 4.
The pyrolysis device further comprises a first fluidization ring 5, a first through hole is formed in the first fluidization ring 5, the first through hole is arranged towards the second reactor, steam produced by the steam providing device in the use process can be sprayed to the second reactor through the first through hole, the sprayed steam can drive the low-temperature low-activity catalyst and the solid heat carrier to be conveyed to the second reaction zone through a gap between the sleeve and the second reactor 12, the low-temperature low-activity catalyst and the solid heat carrier can not be mixed with the high-temperature high-activity catalyst and the solid heat carrier which are input into the second reaction zone at the first time, and the reaction efficiency of the second reaction zone can be improved.
The pyrolysis device further comprises a second fluidization ring 4, a third through hole is formed in the fluidization ring, the third through hole can be arranged towards the first reaction zone, the arrangement of the oil agent distributor 7 is considered, the low-temperature low-activity catalyst and the solid heat carrier in the first reaction zone can be accumulated at the joint of the first reactor 3 and the second reactor 12, the stacked low-temperature low-activity catalyst and solid heat carrier can be impacted by discharging steam through the third through hole, and the low-temperature low-activity catalyst and the solid heat carrier can conveniently enter the second reactor through a gap between the sleeve and the first reactor 3 or the oil agent distributor 7, so that the circulation of the pyrolysis reaction is facilitated.
As shown in fig. 1 and 2, in one possible embodiment, the pyrolysis apparatus further comprises: a first feed pipe 2 which is communicated with the first reactor 3; a conveying pipe 8 connected to one end of the second reactor 12 remote from the first reactor 3; a stripping section through which the transfer tube passes; a settler 10 connected to the other end of the transfer pipe 8; a separator 11 disposed within the settler 10; the waiting inclined tube 16 is communicated with the steam stripping part.
The pyrolysis device further comprises a first feeding pipe 2, and the raw oil is conveniently conveyed into the first reactor 3 through the arrangement of the first feeding pipe 2.
The cracking device also comprises a conveying pipe 8, a stripping part, a settler 10 and a separator 11, after oil gas is subjected to deep cracking in the second reaction zone, the oil gas enters the conveying pipe 8 at the rear part through the second reaction zone, the oil gas is separated from the catalyst through the settler 10 and the separator 11, the oil gas enters a rear part separation system, and the catalyst is gathered to the stripping section 9 and conveyed to the regenerator for regeneration through a waiting inclined pipe 16.
It will be appreciated that the regenerated high temperature, high activity catalyst may be returned to the cracker again for further reaction.
It is understood that the separator 11 may be a cyclone separator 11 of the settler 10.
In one possible embodiment, the pyrolysis apparatus further comprises: the catalytic regeneration system is communicated with the waiting inclined tube 16.
The catalyst can be regenerated through the arrangement of the catalytic regeneration system to form a high-temperature high-activity catalyst, and the high-temperature high-activity catalyst can be returned to the cracking device again for re-reaction.
In one possible embodiment, the pyrolysis apparatus further comprises: a first regeneration chute 17, communicating with the first reactor 3 and the catalytic regeneration system.
The cracking device further comprises a first regeneration chute 17, by which the high-temperature high-activity catalyst output via the catalytic regeneration system can be accepted, and which can be conveyed into the first reactor 3 via the first regeneration chute 17.
As shown in fig. 1 and 2, in one possible embodiment, the pyrolysis apparatus further comprises: a catalyst distributor 13, the catalyst distributor 13 being arranged in the second reactor, the output end of the catalyst distributor 13 being arranged towards the sleeve 6.
The cracking device further comprises a catalyst distributor 13, the catalyst distributor 13 is arranged to facilitate the uniform supply of the high-temperature high-activity catalyst into the second reactor 12, the catalyst distributor 13 is arranged towards the sleeve 6, the high-temperature high-activity catalyst output through the catalyst distributor 13 can be mixed with the oil gas input into the second reactor 12 through the first reactor 3 as soon as possible, and the cracking reaction efficiency can be improved.
In one possible embodiment, the pyrolysis apparatus further comprises: a second regeneration inclined pipe 19 communicated with the catalyst distributor 13; a second feed pipe 20 connected to the second reactor 12 and located between the catalyst distributor 13 and the first reaction vessel; or a third reaction zone riser 14 in communication with the catalyst distributor 13; a third regeneration conduit 18 in communication with the third reaction zone riser 14; a third feed pipe 15 is in communication with the third reaction zone riser 14.
The cracking unit may further comprise a second regeneration chute 19, whereby the second regeneration chute 19 is arranged to deliver high temperature, high activity catalyst to the second reactor 12, it being understood that the second regeneration chute 19 may equally be connected to a catalytic regeneration system.
The pyrolysis device can also comprise a second feeding pipe 20, and can recycle C4 and light gasoline, and the oil gas separated from the C4 and/or light gasoline by the second feeding pipe 20 and the oil agent distributor 7 at the outlet of the first reaction zone is contacted and mixed with part of low-temperature catalyst
The pyrolysis device may further comprise a third regeneration inclined tube 18 and a third feeding tube 15, and C4 and light gasoline may be recycled for improving the yield of low-carbon olefin. The mode of recycling the C4 and the light gasoline is determined according to the proper conveying mode of the high-temperature regenerated catalyst/high-temperature solid heat carrier. A third regeneration inclined tube 18 and a third feeding tube 15 can be arranged, the high-temperature regenerated catalyst/high-temperature solid heat carrier is lifted to a second reaction zone through the third regeneration inclined tube 18 by C4 and light gasoline gasification, cracking reaction is carried out in the lifting process, then the cracking reaction is carried out in an annular fluidized bed and intermediate components such as liquefied gas, gasoline, diesel oil and the like, and at the moment, the third reaction zone in the third regeneration inclined tube 18 is a lifting tube and an annular fluidized bed; when the high temperature regenerated catalyst/high temperature solid heat carrier can be directly conveyed (without lifting) to the second reaction zone, the recycled C4 and light gasoline can be directly fed in an annular fluidized bed, and the third reaction zone is the annular fluidized bed.
By the pyrolysis device, the reaction temperatures of the first reaction zone and the second reaction zone are respectively controlled by the circulation amount of the regenerated catalyst/the solid heat carrier entering the respective reaction zones, so that the aim of independently controlling the reaction temperatures of the different reaction zones is fulfilled. The method realizes the zonal reaction of raw materials with different properties according to the respective reaction mechanism requirements, realizes the independent control of the temperatures of different reaction areas, can obviously reduce the yields of byproducts such as dry gas, coke and the like, improves the yields and selectivity of low-carbon olefin, and can flexibly adjust the yields of ethylene and propylene.
According to the embodiment of the application, the raw materials with different properties can be subjected to partition reaction according to respective reaction mechanisms, so that the temperature of different reaction areas can be independently controlled. The oil agent distributor 7 is arranged, so that part of low-temperature low-activity catalyst/low-temperature solid heat carrier can be shunted from the outside of the sleeve 6, the low-temperature low-activity catalyst/low-temperature solid heat carrier rising inside the sleeve 6 is reduced, and a high-severity reaction zone is easily formed by mixing the oil agent distributor with the high-temperature high-activity catalyst/high-temperature solid heat carrier, so that the cracking reaction is promoted; meanwhile, oil gas can be restrained on the inner section of the sleeve 6, the high-temperature high-activity catalyst/high-temperature solid heat carrier is distributed above the sleeve 6 along the section of the sleeve 6, and the downward-sprayed high-temperature high-activity catalyst/high-temperature solid heat carrier is in reverse contact with rising oil gas, so that the back mixing effect is enhanced; the high-temperature high-activity catalyst/high-temperature solid heat carrier is distributed at the middle part of the section of the bed layer in the second reaction zone, so that the reaction efficiency reduction caused by the sliding effect of the side wall of the bed layer can be reduced, and favorable conditions are created for the high-severity reaction in the second reaction zone.
The first reaction zone adopts lower severity reaction conditions; the second reaction zone is supplemented with a high-temperature high-activity catalyst/high-temperature solid heat carrier to form a high-severity reaction zone; the method can obviously reduce the yield of byproducts such as dry gas, coke and the like, improve the yield and selectivity of the low-carbon olefin, and simultaneously realize flexible adjustment of the yields of ethylene and propylene by adjusting the temperature of the second reaction zone.
According to a second aspect of embodiments of the present application, there is provided a pyrolysis apparatus for any one of the above technical solutions, the pyrolysis method includes:
controlling the feed rate of the raw oil so that the residence time of the raw oil in the first reaction zone is 1s to 2s and the residence time of the oil gas in the second reaction zone is 2s to 5s;
wherein the reaction temperature of the first reaction zone is 550 ℃ to 600 ℃, and the reaction temperature of the second reaction zone is 630 ℃ to 730 ℃.
By means of the cracking method, the cracking device can conduct partition reaction according to the respective reaction mechanisms aiming at raw materials with different properties, and temperature independent control of different reaction areas is achieved. The annular fluidized bed is arranged, so that part of low-temperature low-activity catalyst/low-temperature solid heat carrier can be shunted from the outside of the sleeve, the low-temperature low-activity catalyst/low-temperature solid heat carrier rising in the sleeve is reduced, and a high-severity reaction zone is easily formed by mixing the catalyst/low-temperature solid heat carrier with the high-temperature high-activity catalyst/high-temperature solid heat carrier, so that cracking reaction is promoted; meanwhile, oil gas can be restrained on the inner section of the sleeve, the high-temperature high-activity catalyst/high-temperature solid heat carrier is distributed above the sleeve along the section of the sleeve, and the downward-sprayed high-temperature high-activity catalyst/high-temperature solid heat carrier is in reverse contact with rising oil gas, so that the back mixing effect is enhanced; the high-temperature high-activity catalyst/high-temperature solid heat carrier is distributed at the middle part of the section of the bed layer in the second reaction zone, so that the reaction efficiency reduction caused by the sliding effect of the side wall of the bed layer can be reduced, and favorable conditions are created for the high-severity reaction in the second reaction zone.
Example 1
See fig. 1. The regenerated catalyst/solid heat carrier from the first regeneration inclined tube is lifted by a lifter, contacts with a first feeding pipe, is gasified and reacts, and enters an oil agent distributor at the outlet of a first reaction zone at the tail end of the first reactor to distribute and initially separate oil gas from the low-temperature low-activity catalyst/low-temperature solid heat carrier. C4 and/or light gasoline are/is contacted, gasified and reacted with regenerated catalyst/solid heat carrier from a third regeneration inclined tube through a third feeding tube, are distributed to a catalyst/solid heat carrier catalyst distributor through a third reaction zone riser, are contacted and mixed with oil gas and partial low-temperature catalyst separated from an oil agent distributor at the outlet of a first reaction zone, and the other partial low-temperature catalyst is fluidized and conveyed to a second reactor through a first fluidization ring outside the sleeve through an outer annular cavity of the sleeve for contact and mixing, and the oil gas is deeply cracked in the second reaction zone. The oil gas enters a rear conveying pipe through a second reaction zone, the oil gas and the catalyst are separated through a separator, the oil gas enters a rear separation system, the catalyst is collected to a stripping section, and the catalyst is conveyed to a regenerator through a waiting inclined pipe for regeneration.
Example 2
See fig. 2. The regenerated catalyst/solid heat carrier from the first regeneration inclined tube is lifted by a lifter, contacts with a first feeding pipe, is gasified and reacts, enters an oil solution distributor at the outlet of a first reaction zone at the tail end through a first reactor, and distributes and primarily separates oil gas from the low-temperature low-activity catalyst/low-temperature solid heat carrier. The regenerated catalyst/solid heat carrier from the second regeneration inclined tube is conveyed to a regenerated catalyst/solid heat carrier catalyst distributor for distribution, and is contacted and mixed with the C4 and/or light gasoline and part of low-temperature catalyst separated by the second feed pipe and the first reaction zone outlet oil agent distributor, and the other part of low-temperature catalyst is conveyed to the second reaction zone for contact and mixing through the sleeve external annular cavity and the sleeve external first fluidization ring in a fluidization way, and the oil gas is subjected to deep cracking in the second reaction zone. The oil gas enters a rear conveying pipe through a second reaction zone, the oil gas and the catalyst are separated through a separator, the oil gas enters a rear separation system, the catalyst is collected to a stripping section, and the catalyst is conveyed to a regenerator through a waiting inclined pipe for regeneration.
Comparative example
The existing catalytic cracking process is used, namely, a reaction technology that a riser is connected with a fluidized bed in series is adopted.
The reaction conditions and product distribution of the comparative examples are shown in Table 1.
Table 1 comparison of reaction conditions and product distribution for comparative and example
As can be seen from the data in the table, the propylene yield and selectivity are greatly increased by adopting the method, and the dry gas and coke yield are greatly reduced. Example 1 the third reaction zone has more riser reactors than example 2, and the propylene yield and selectivity of example 1 is higher.
In the present invention, the terms "first," "second," "third," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance; the term "plurality" means two or more, unless expressly defined otherwise. The terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; "coupled" may be directly coupled or indirectly coupled through intermediaries. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the description of the present invention, it should be understood that the directions or positional relationships indicated by the terms "upper", "lower", "left", "right", "front", "rear", etc. are based on the directions or positional relationships shown in the drawings, are merely for convenience of describing the present invention and simplifying the description, and do not indicate or imply that the devices or units referred to must have a specific direction, be constructed and operated in a specific direction, and thus should not be construed as limiting the present invention.
In the description of the present specification, the terms "one embodiment," "some embodiments," "particular embodiments," and the like, mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A pyrolysis apparatus, comprising:
a first reactor having a first reaction zone formed therein;
the second reactor, one end of the said first reactor locates at the inside of the said second reactor, there is a second reaction zone in the said second reactor;
the sleeve is sleeved at one end of the first reactor, which is positioned in the second reactor, and a gap is reserved between the outer wall of the sleeve and the second reactor;
an oil distributor is disposed between the sleeve and the first reactor.
2. The pyrolysis apparatus of claim 1 wherein the oil dispenser comprises:
the distribution pipe is provided with a first through hole;
wherein, oil agent distributor is a plurality of.
3. A pyrolysis apparatus as recited in claim 1, wherein,
the first reactor comprises: a fluidized bed reactor or riser reactor;
the second reactor is a dense phase fluidized bed.
4. A pyrolysis apparatus according to any one of claims 1 to 3, further comprising:
and the lifter is connected with one end of the first reactor, which is away from the second reactor.
5. A pyrolysis apparatus according to any one of claims 1 to 3, further comprising:
the first fluidization ring is provided with a second through hole, and is arranged in the second reactor and positioned between the sleeve and the second reactor;
the second fluidization ring is provided with a third through hole, and the second fluidization ring is arranged at one end of the first reactor, which is close to the second reactor;
and a steam supply device communicated with the first fluidization ring and the second fluidization ring.
6. A pyrolysis apparatus according to any one of claims 1 to 3, further comprising:
the first feeding pipe is communicated with the first reactor;
the conveying pipe is connected to one end, far away from the first reactor, of the second reactor;
a stripping section through which the transfer pipe passes;
a settler connected to the other end of the delivery pipe;
a separator disposed within the settler;
and the waiting inclined tube is communicated with the stripping part.
7. The pyrolysis apparatus of claim 6, further comprising:
the catalytic regeneration system is communicated with the waiting inclined tube;
and the first regeneration inclined pipe is communicated with the first reactor and the catalytic regeneration system.
8. A pyrolysis apparatus according to any one of claims 1 to 3, further comprising:
and a catalyst distributor, wherein the catalyst distributor is arranged in the second reactor, and the output end of the catalyst distributor is arranged towards the sleeve.
9. The pyrolysis apparatus of claim 8, further comprising:
a second regeneration chute, which is communicated with the catalyst distributor;
the second feeding pipe is communicated with the second reactor and is positioned between the catalyst distributor and the first reactor; or (b)
A third reaction zone riser in communication with the catalyst distributor;
the third regeneration inclined tube is communicated with the third reaction zone lifting tube;
and the third feeding pipe is communicated with the third reaction zone lifting pipe.
10. A cracking process for a cracking apparatus according to any one of claims 1 to 9, comprising:
the feed rate of the raw oil is controlled so that the residence time of the raw oil in the first reaction zone is 1s to 2s, and the residence time of the oil gas in the second reaction zone is 2s to 5s;
wherein the reaction temperature of the first reaction zone is 550 ℃ to 600 ℃, and the reaction temperature of the second reaction zone is 630 ℃ to 730 ℃.
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CN118344895A (en) * | 2024-06-17 | 2024-07-16 | 江苏博颂能源科技有限公司 | Fluidization ring of catalytic cracking device settler |
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CN118344895A (en) * | 2024-06-17 | 2024-07-16 | 江苏博颂能源科技有限公司 | Fluidization ring of catalytic cracking device settler |
CN118344895B (en) * | 2024-06-17 | 2024-10-22 | 江苏博颂能源科技有限公司 | Fluidization ring of catalytic cracking device settler |
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