CN102875290B - Reaction unit for preparing low-carbon olefins by using methanol and naphtha - Google Patents
Reaction unit for preparing low-carbon olefins by using methanol and naphtha Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention relates to a reaction unit for preparing low-carbon olefins by using methanol and naphtha, mainly solving the problem of low yield of low-carbon olefins in the prior art. The reaction unit disclosed herein mainly comprises a first reaction zone 19, a second reaction zone 10, a third reaction zone 12, a fourth reaction zone 23, a disengager 17, an a regenerator 3, the outlets of the first reaction zone 19 and the third reaction zone 12 are all connected with the disengager 17, the outlet of the second reaction zone 10 is connected with the bottom of the third reaction zone 12, the outlet of the fourth reaction zone 23 is connected with the third reaction zone 12, the bottoms of the first reaction zone 19, the second reaction zone 10 and the fourth reaction zone 23 are all provided with catalyst inlets which are connected with the regenerator 3 through regeneration inclined pipes, the bottom of the disengager is connected with a stripper 18, and the bottom of the stripper 18 is provided with a regeneration standpipe 11 which is connected with the regenerator 3. The reaction unit disclosed herein well solves the problem and can be used in the industrial production of low-carbon olefins.
Description
Technical field
The present invention relates to a kind of reaction unit of being prepared low-carbon alkene by methyl alcohol and petroleum naphtha.
Technical background
Low-carbon alkene, ethene and propylene, be two kinds of important basic chemical industry raw materials, its demand is in continuous increase.Usually, ethene, propylene are to produce by petroleum path, but due to the limited supply of petroleum resources and higher price, the cost of being produced ethene, propylene by petroleum resources constantly increases.In recent years, people start to greatly develop the technology that alternative materials transforms ethene processed, propylene.Wherein, the important alternative materials for light olefin production of one class is oxygenatedchemicals, such as alcohols (methyl alcohol, ethanol), ethers (dme, methyl ethyl ether), ester class (methylcarbonate, methyl-formiate) etc., these oxygenatedchemicalss can be transformed by coal, Sweet natural gas, biomass equal energy source.Some oxygenatedchemicals can reach fairly large production, as methyl alcohol, can be made by coal or Sweet natural gas, and technique is very ripe, can realize the industrial scale of up to a million tonnes.Popularity due to oxygenatedchemicals source, add and transform the economy that generates light olefin technique, so by the technique of oxygen-containing compound conversion to produce olefine (OTO), particularly the technique by preparing olefin by conversion of methanol (MTO) is subject to increasing attention.
Petroleum naphtha is a kind of light-end products, by crude distillation or oil secondary processing, is cut corresponding cut and is obtained.Its boiling spread is determined according to need, is generally wider boiling range, as 20-220 ℃.Petroleum naphtha is pyrolysis in tubular furnace preparing ethylene, and propylene and catalytic reforming are produced the important source material of benzene,toluene,xylene.As cracking stock, require petroleum naphtha form in the content of alkane and naphthenic hydrocarbon be not less than 70% (volume).Naphtha catalytic pyrolysis preparing low-carbon alkene is under the condition existing at catalyzer, and petroleum hydrocarbon is carried out to the production process that cracking obtains low-carbon alkene.With traditional tube furnace steam heat cracking, compare, this process reaction temperature is approximately lower 50～200 ℃ than steam cracking reaction, and energy consumption significantly reduces; Cracking furnace pipe inwall coking rate also can reduce, thereby can prolong operation cycle, increases the boiler tube life-span; Carbon emission simultaneously also can reduce, and has alleviated pollution, and can adjust the product mix flexibly.
Technology and reactor that a kind of oxygenate conversion is low-carbon alkene in US6166282, have been announced, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu of gas speed has reacted, rise to after the fast subregion that internal diameter diminishes rapidly, adopt special gas-solid separation equipment initial gross separation to go out most entrained catalyst.Due to reaction after product gas and catalyzer sharp separation, effectively prevented the generation of secondary reaction.Through analog calculation, to compare with traditional bubbling fluidization bed bioreactor, this fast fluidized bed reactor internal diameter and the required reserve of catalyzer all greatly reduce.
The multiple riser reaction unit of having announced in CN1723262 with central catalyst return is low-carbon alkene technique for oxygenate conversion, this covering device comprises a plurality of riser reactors, gas solid separation district, a plurality of offset components etc., each riser reactor has the port of injecting catalyst separately, be pooled to the disengaging zone of setting, catalyzer and gas product are separated.But there is the shortcoming that yield of light olefins is lower in the method.
In EP0448000 and EP0882692, announced a kind of method of methanol production propylene, first methyl alcohol be converted into DME and water, then mixture is transported to First reactor, and adds steam in this reactor.In the first reactor, methyl alcohol and (or) dme or its mixture contact and react with catalyzer, catalyzer adopts the special-purpose ZSM-5 catalyzer containing ZnO and CdO, 280～570 ℃ of temperature of reaction, pressure 0.01～0.1MPa, prepares and take the product that propylene is main hydro carbons.Heavier product is as C
5 +hydrocarbon continues to react in second reactor to be converted into take propylene as main hydro carbons, sends separator after cooling back to.Product is compressed, can obtain purity after further refining is 97% chemical grade propylene.But in this technique, adopt a plurality of fixed-bed reactor, due to the activity restriction of catalyzer, therefore need frequent blocked operation, and heat-obtaining problem is also very complicated.
US 20070083071 has announced the processing method that a kind of hydrocarbon catalytic pyrolysis is produced ethene, propylene, hydrocarbon feed is converted into the product that comprises low-carbon alkene in catalytic cracker, then product stream is separated into C2～C3 alkane, C2～C3 alkene, three kinds of logistics of C4+ hydrocarbon by series of process, C2～C3 alkane is returned to tube cracking furnace and carry out thermo-cracking, C4+ hydrocarbon returns to catalytic cracker and carries out catalytic pyrolysis, finally obtains ethene, the propylene product of higher yields.The method adopts riser reactor, and reactant residence time is shorter, and low-carbon alkene product once through yield is lower.
Due to the reaction of naphtha catalytic cracking and preparing olefin by conversion of methanol object product---low-carbon alkene is identical, and the main ingredient kind in product is roughly the same separately, the catalyst system adopting is also roughly the same, and from reaction mechanism angle, all have the process that is cracked into small molecules hydro carbons by macromole hydrocarbon or intermediate, so these two kinds of Technologies are had ready conditions and are coupled.The present invention has solved this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the not high problem of yield of light olefins existing in prior art, and a kind of new reaction unit of being prepared low-carbon alkene by methyl alcohol and petroleum naphtha is provided.This device, for the production of low-carbon alkene, has advantages of that yield of light olefins is higher.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of reaction unit of being prepared low-carbon alkene by methyl alcohol and petroleum naphtha, mainly comprise the first reaction zone 19, second reaction zone 10, the 3rd reaction zone 12, the 4th reaction zone 23, settling vessel 17, revivifier 3, the first reaction zone 19, the 3rd reaction zone 12 outlets are all connected with settling vessel 17, second reaction zone 10 outlets are connected with 12 bottoms, the 3rd reaction zone, the 4th reaction zone 23 outlets are connected with the 3rd reaction zone 12, the first reaction zone 19, second reaction zone 10, the 4th 23 bottoms, reaction zone is equipped with catalyst inlet and by regenerator sloped tube, is connected with revivifier 3 respectively, settling vessel 17 bottoms are connected with stripper 18, stripper 18 bottoms are provided with regeneration standpipe 11 and are connected with revivifier 3.
In technique scheme, described catalyzer comprises ZSM-5 molecular sieve, SiO
2/ Al
2o
3mol ratio is 10～100; Described the first reaction zone 19 is riser tube; Second reaction zone 10 is riser tube; The 3rd reaction zone 12 is fast bed; The 4th reaction zone 23 is riser tube; Described settling vessel 17 inside are provided with gas-solid cyclone separator 25; Described the first reaction zone 19, the 3rd reaction zone 12 outlets are equipped with slightly and revolve; On described the first reaction zone 19, the 4th reaction zone 23 axial direction dues, at least one opening for feed 9 is respectively set; Described settling vessel 17 tops are provided with product gas outlet 22, and revivifier 3 tops are provided with exhanst gas outlet 16.
In the present invention, the catalyzer coke content massfraction after described regeneration is 0.01～0.5%; In described the first reaction zone feeds, except petroleum naphtha, also comprise water vapour, the weight ratio of water vapour and petroleum naphtha is 0.05～1.5: 1; In the 3rd reaction zone feeds, be mainly methyl alcohol; Described petroleum naphtha boiling range is between 20 ℃～220 ℃; In described the first reaction zone, reaction conditions is: temperature of reaction is 570～670 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 4～10 meter per seconds; In second reaction zone, reaction conditions is: temperature of reaction is 480～600 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 4～10 meter per seconds; In the 3rd reaction zone, reaction conditions is: temperature of reaction is 480～600 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 1～3 meter per second; In the 4th reaction zone, reaction conditions is: temperature of reaction is 530～630 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 4～10 meter per seconds; The logistics of the isolated C4～C8 of centrifugal station hydrocarbon mixture is from the 4th bottom, reaction zone or enter the 4th reaction zone from least one opening for feed in axial direction separating; Catalyst activity sex index after regeneration is greater than 0.8; Catalyzer after regeneration is divided into three parts, and 20～40% weight enter the first reaction zone, and 20～40% weight enter second reaction zone, and 20～60% weight enter the 4th reaction zone,
Regenerated catalyst activity index is for embodying the regeneration level of decaying catalyst, take live catalyst as benchmark, the amount that transforms light naphthar with each catalyzer under rigid condition is carried out relatively, and method of calculation are: regenerated catalyst activity index=(the light naphthar amount that under light naphthar amount/certain condition that under certain condition, regenerated catalyst transforms, live catalyst transforms) * 100%.Described certain condition or rigid condition refer to employing fluidized-bed reactor, in temperature of reaction, are that 600 ℃, reaction pressure be take the reaction conditions that gauge pressure counts 0, the gas phase residence time is 4 seconds.
ZSM-5 molecular sieve of the present invention can adopt method known in the field, as hydrothermal synthesis method, be prepared, on described molecular sieve catalyst, understand the metal that optionally load has dehydrogenation functionality, the metal of dehydrogenation functionality is selected from least one in IB in the periodic table of elements, IIB, VB, VIB, VIIB or VIII family, and the method on ZSM-5 molecular sieve can adopt method known in the field by the metal load of dehydrogenation functionality, as pickling process or coprecipitation method.After the ZSM-5 molecular sieve of load dehydrogenation functionality metal prepares, add binding agent, make mixed slurry, adopt spray drying process to carry out drying and moulding, then the catalyst fines after moulding is placed in to stoving oven and carries out roasting, obtain catalyst sample after cooling.Binding agent can be selected SiO
2, Al
2o
3deng.
Adopt device of the present invention, four reaction areas is set, it is low-carbon alkene that the first reaction zone is mainly used in naphtha catalytic cracking, second reaction zone is mainly used in transforming methyl alcohol, the 3rd reaction zone is mainly used in transforming the gaseous substance in second reaction zone and the 4th reaction zone, and the 4th reaction zone is mainly used in transforming C4～C8 hydrocarbon mixture by product, and in the first reaction zone, the 4th reaction zone adopts axial admission mode, reduce raw material dividing potential drop, to improving low-carbon alkene transformation efficiency.In the present invention, settling vessel and revivifier can be arranged apart or the public settling vessel in first, second, third, fourth reaction zone can be coaxially set.The 4th reaction zone provides reactant and catalyzer for the 3rd reaction zone, and play is the object of the 3rd reaction zone cooling simultaneously.Therefore, adopt device of the present invention, not only realize energy-optimisedly, and methyl alcohol and petroleum naphtha are transformed and prepare low-carbon alkene and be coupled, transform the high-carbon hydrocarbon by product that falls to generate simultaneously, reached the object that improves selectivity of light olefin.
Adopt technical scheme of the present invention: described catalyzer comprises ZSM-5 molecular sieve, SiO
2/ Al
2o
3mol ratio is 10～100; Described the first reaction zone 19 is riser tube; Second reaction zone 10 is riser tube; The 3rd reaction zone 12 is fast bed; The 4th reaction zone 23 is riser tube; Described settling vessel 17 inside are provided with gas-solid cyclone separator 25; Described the first reaction zone 19, the 3rd reaction zone 12 outlets are equipped with slightly and revolve; On described the first reaction zone 19, the 4th reaction zone 23 axial direction dues, at least one opening for feed 9 is respectively set; Described settling vessel 17 tops are provided with product gas outlet 22, and revivifier 3 tops are provided with exhanst gas outlet 16, and low-carbon alkene carbon base absorption rate can reach 65.06% weight, has obtained good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of device of the present invention.
In Fig. 1,1 is regenerating medium source line; 2 is plug valve to be generated; 3 is revivifier; 4 is buffer zone; 5 is regenerator sloped tube delivering vapor entrance; 6 is second reaction zone charging; 7 is the 4th reaction zone feeds; 8 is buffer zone; 9 is the first reaction zone and the 4th reaction zone side feed opening; 10 is second reaction zone; 11 is regeneration standpipe; 12 is the 3rd reaction zone; 13 is stripping medium inlet pipeline; 14 is that the first reaction zone outlet is slightly revolved; 15 is gas-solid cyclone separator; 16 is exhanst gas outlet; 17 is settling vessel; 18 is stripper; 19 is the first reaction zone; 20 is that the 3rd reaction zone outlet is slightly revolved; 21 is the first reaction zone feeds; 22 is products export pipeline; 23 is the 4th reaction zone; 24 is the 3rd reaction zone feeds; 25 is gas-solid cyclone separator; 26 is regenerator sloped tube; 27 is regenerator sloped tube; 28 is regenerator sloped tube; 29 is buffer zone.
The raw material that comprises petroleum naphtha from 19 bottoms, the first reaction zone or at least one position of at least one opening for feed 9 separating along the first reaction zone axial direction due enter the first reaction zone 19, the product stream of generation and catalyzer enter settling vessel 17, the raw material that comprises methyl alcohol enters second reaction zone 10, the product stream and the catalyzer that generate enter the 3rd reaction zone 12, product stream and catalyzer that the 3rd reaction zone 12 generates enter settling vessel 17, in settling vessel 17, after gaseous stream and catalyst separating, enter centrifugal station, isolate and comprise low-carbon alkene, the product of C4～C8 hydrocarbon mixture, logistics comprising C4～C8 hydrocarbon mixture enters the 4th reaction zone 23, the product stream and the catalyzer that generate enter the 3rd reaction zone 12, in settling vessel 17, catalyzer enters revivifier 3 regeneration after stripping, catalyzer after regeneration is divided into three parts, a part enters the first reaction zone 19, a part enters second reaction zone 10, a part enters the 4th reaction zone 23.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
In reaction unit as shown in Figure 1, catalyzer is ZSM-5, SiO
2/ Al
2o
3mol ratio is 100, and in catalyzer, binding agent mass content is 45%, and binding agent is SiO
2, ZSM-5 molecular sieve mass content is 45%, loaded Cu/Zn/Co, and the percentage ratio that loaded metal quality accounts for catalyst quality is Cu:5.53; Zn:2.76; Co:1.68.The raw material that comprises petroleum naphtha enters the first reaction zone from the first bottom, reaction zone, and product stream and the catalyzer of generation enter settling vessel, the raw material of methyl alcohol enters second reaction zone, the product stream and the catalyzer that generate enter the 3rd reaction zone, product stream and catalyzer that the 3rd reaction zone generates enter settling vessel, in settling vessel, after gaseous stream and catalyst separating, enter centrifugal station, isolate and comprise low-carbon alkene, the product of C4～C8 hydrocarbon mixture, wherein the logistics of C4～C8 hydrocarbon mixture enters the 4th reaction zone, the product stream and the catalyzer that generate enter the 3rd reaction zone, in settling vessel, catalyzer enters revivifier regeneration after stripping, catalyzer after regeneration is divided into three parts, 20% weight enters the first reaction zone, 20% weight enters second reaction zone, 60% weight enters the 4th reaction zone.The first reaction zone is riser tube; Second reaction zone is riser tube; The 3rd reaction zone is fast bed; The 4th reaction zone is riser tube.Catalyzer coke content massfraction after regeneration is in 0.01%, the first reaction zone feeds, also to comprise that water vapour, the weight ratio of water vapour and petroleum naphtha are 1.5: 1, in the 3rd reaction zone feeds, is methyl alcohol, and petroleum naphtha forms in Table 1.In the first reaction zone, reaction conditions is: temperature of reaction is 570 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds; In second reaction zone, reaction conditions is: temperature of reaction is 480 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds; In the 3rd reaction zone, reaction conditions is: temperature of reaction is 482 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 1 meter per second; In the 4th reaction zone, reaction conditions is: temperature of reaction is 530 ℃, and reaction pressure is counted 0.01～MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds.The logistics of C4～C8 hydrocarbon mixture enters the 4th reaction zone from the 4th bottom, reaction zone.Catalyst activity sex index after regeneration is 0.93.Methyl alcohol and naphtha feed weight ratio are 1: 1.The stability that keeps catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 59.28% weight.
Table 1 petroleum naphtha typical case form
| Initial boiling point, ℃ | 40 |
| Final boiling point, ℃ | 162 |
| Positive structure and isoparaffin, % by weight | 65.18 |
| Alkene, % by weight | 0.17 |
| Naphthenic hydrocarbon, % by weight | 28.44 |
| Aromatic hydrocarbons, % by weight | 6.21 |
[embodiment 2]
According to condition and the step described in embodiment 1, catalyzer is ZSM-5, SiO
2/ Al
2o
3mol ratio is 10, and the raw material that comprises petroleum naphtha is from the first bottom, reaction zone and enter the first reaction zone along an opening for feed the first reaction zone axial direction due, and this opening for feed distance first bottom, reaction zone is 1/2 first reaction zone height.Catalyzer after regeneration is divided into three parts, and 40% weight enters the first reaction zone, and 40% weight enters second reaction zone, and 20% weight enters the 4th reaction zone.Catalyzer coke content massfraction after regeneration is in 0.5%, the first reaction zone feeds, also to comprise that water vapour, the weight ratio of water vapour and petroleum naphtha are 0.05: 1.In the first reaction zone, reaction conditions is: temperature of reaction is 670 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds; In second reaction zone, reaction conditions is: temperature of reaction is 600 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds; In the 3rd reaction zone, reaction conditions is: temperature of reaction is 600 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 3 meter per seconds; In the 4th reaction zone, reaction conditions is: temperature of reaction is 630 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds.The logistics of C4～C8 hydrocarbon mixture is from the 4th bottom, reaction zone and enter the 4th reaction zone from an opening for feed of in axial direction, and this opening for feed distance the 4th bottom, reaction zone is 1/2 the 4th reaction zone height.Catalyst activity sex index after regeneration is 0.8.The stability that keeps catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 62.49% weight.
[embodiment 3]
According to condition and the step described in embodiment 1, catalyzer is ZSM-5, SiO
2/ Al
2o
3mol ratio is 70, and the raw material that comprises petroleum naphtha is from the first bottom, reaction zone and enter the first reaction zone along two opening for feeds the first reaction zone axial direction due, and two opening for feeds distance the first bottoms, reaction zones are respectively 1/3,1/2 first reaction zone height.Catalyzer after regeneration is divided into three parts, and 30% weight enters the first reaction zone, and 30% weight enters second reaction zone, and 40% weight enters the 4th reaction zone.Catalyzer coke content massfraction after regeneration is in 0.05%, the first reaction zone feeds, also to comprise that water vapour, the weight ratio of water vapour and petroleum naphtha are 0.5: 1.In the first reaction zone, reaction conditions is: temperature of reaction is 650 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 7 meter per seconds; In second reaction zone, reaction conditions is: temperature of reaction is 560 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 6 meter per seconds; In the 3rd reaction zone, reaction conditions is: temperature of reaction is 550 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 6.3 meter per seconds; In the 4th reaction zone, reaction conditions is: temperature of reaction is 610 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 7 meter per seconds.The logistics of C4～C8 hydrocarbon mixture is from the 4th bottom, reaction zone and enter the 4th reaction zone from two opening for feeds in axial direction, and two opening for feed distance the 4th bottoms, reaction zone are respectively 1/3,1/2 the 4th reaction zone height.Catalyst activity sex index after regeneration is 0.94.The stability that keeps catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 65.06% weight.
[embodiment 4]
According to condition and the step described in embodiment 1, catalyzer is ZSM-5, SiO
2/ Al
2o
3mol ratio is 30, and the raw material that comprises petroleum naphtha is from the first bottom, reaction zone and enter the first reaction zone along three opening for feeds the first reaction zone axial direction due, and three opening for feeds distance the first bottoms, reaction zones are respectively 1/4,1/3,1/2 first reaction zone height.Catalyzer after regeneration is divided into three parts, and 33% weight enters the first reaction zone, and 40% weight enters second reaction zone, and 27% weight enters the 4th reaction zone.Catalyzer coke content massfraction after regeneration is in 0.1%, the first reaction zone feeds, also to comprise that water vapour, the weight ratio of water vapour and petroleum naphtha are 0.25: 1.In the first reaction zone, reaction conditions is: temperature of reaction is 660 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; In second reaction zone, reaction conditions is: temperature of reaction is 570 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; In the 3rd reaction zone, reaction conditions is: temperature of reaction is 560 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 4.8 meter per seconds; In the 4th reaction zone, reaction conditions is: temperature of reaction is 615 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds.The logistics of C4～C8 hydrocarbon mixture is from the 4th bottom, reaction zone and enter the 4th reaction zone from two opening for feeds in axial direction, and two opening for feed distance the 4th bottoms, reaction zone are respectively 1/3,1/2 the 4th reaction zone height.Catalyst activity sex index after regeneration is 0.94.The stability that keeps catalyst flow control, gas product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 60.67% weight.
[comparative example 1]
According to condition and the step described in embodiment 1, just the 4th reaction zone is not set, low-carbon alkene carbon base absorption rate is 52.69% weight.
[comparative example 2]
According to condition and the step described in embodiment 1, the 3rd reaction zone and the 4th reaction zone are not just set, low-carbon alkene carbon base absorption rate is 47.28% weight.
Obviously, adopt device of the present invention, can reach the object that improves yield of light olefins, there is larger technical superiority, can be used in the industrial production of low-carbon alkene.
Claims (6)
1. a reaction unit of being prepared low-carbon alkene by methyl alcohol and petroleum naphtha, described low-carbon alkene is ethene and propylene, mainly comprise the first reaction zone (19), second reaction zone (10), the 3rd reaction zone (12), the 4th reaction zone (23), settling vessel (17), revivifier (3), the first reaction zone (19), the 3rd reaction zone (12) outlet is all connected with settling vessel (17), second reaction zone (10) outlet is connected with the 3rd bottom, reaction zone (12), the 4th reaction zone (23) outlet is connected with the 3rd reaction zone (12), the first reaction zone (19), second reaction zone (10), the 4th bottom, reaction zone (23) is equipped with catalyst inlet and by regenerator sloped tube, is connected with revivifier (3) respectively, settling vessel (17) bottom is connected with stripper (18), stripper (18) bottom is provided with regeneration standpipe (11) and is connected with revivifier (3).
2. by methyl alcohol and petroleum naphtha, prepared according to claim 1 the reaction unit of low-carbon alkene, it is characterized in that described the first reaction zone (19) is for riser tube; Second reaction zone (10) is riser tube; The 3rd reaction zone (12) is fast bed; The 4th reaction zone (23) is riser tube.
3. by methyl alcohol and petroleum naphtha, prepared according to claim 1 the reaction unit of low-carbon alkene, it is characterized in that described settling vessel (17) inside is provided with gas-solid cyclone separator (25).
4. by methyl alcohol and petroleum naphtha, prepared according to claim 1 the reaction unit of low-carbon alkene, it is characterized in that described the first reaction zone (19), the 3rd reaction zone (12) outlet are equipped with slightly and revolve.
5. by methyl alcohol and petroleum naphtha, prepared according to claim 1 the reaction unit of low-carbon alkene, it is characterized in that, on described the first reaction zone (19), the 4th reaction zone (23) axial direction due, at least one opening for feed (9) is respectively set.
6. by methyl alcohol and petroleum naphtha, prepared according to claim 1 the reaction unit of low-carbon alkene, it is characterized in that described settling vessel (17) top is provided with product gas outlet (22), revivifier (3) top is provided with exhanst gas outlet (16).
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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