CN104877703A - Alkane catalytic conversion method and reactor thereof - Google Patents
Alkane catalytic conversion method and reactor thereof Download PDFInfo
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Abstract
The invention relates to an alkane catalytic conversion method and a reactor thereof. The alkane catalytic conversion method comprises the following step: contacting an alkane raw material with a catalyst in a fluidized bed reactor in a reflux mode to perform catalytic conversion reaction, wherein the alkane raw material is one or more of C1-C8 alkanes, natural gas or light naphtha. The alkane catalytic conversion reactor comprises the fluidized bed reactor, wherein the upper part of the fluidized bed reactor is provided with a catalyst guide device, and the lower part of the fluidized bed reactor is provided with an alkane raw material guide device. The alkane catalytic conversion method or alkane catalytic conversion reactor for performing alkane catalytic conversion reaction can enhance the conversion rate of the alkane raw material and the selectivity of the target product.
Description
Technical field
The invention belongs to refining of petroleum field, be specifically related to a kind of alkanes catalysis conversion method and conversion unit thereof.
Background technology
Fluid catalytic cracking (FCC) technology is one of Main Means of crude oil secondary processing, and its process-technology-evolutions is relatively ripe, the gasoline of domestic market 70 ~ 80%, and the diesel oil of 30% adopts fluid catalytic cracking (FCC) technology.Along with the change of raw material and the development of complete processing, its technical process and processing units also constantly to occur to improve.But up to now, the reactor of fluidized catalytic cracker (FCCU) nearly all both at home and abroad all adopts riser reactor, comprising upstriker riser reactor and downstriker riser reactor.
Mix in upstriker riser reactor bottom with the catalyzer from revivifier at upstriker riser reactor Raw oil and flow up along upstriker riser tube, under the oily effect at catalyzer of the process Raw of rising, cracking reaction occurring.The patented technology of upstriker riser reactor being carried out to component home improvement is a lot, as heavy oil feed (nozzle) atomization technique; Upstriker riser reactor end gas-solid quickly separating technology; Spent agent high-efficiency multi-section steam stripping technique; Two sections of highly efficient regeneration technology; Upstriker riser tube reaction terminating technology; Sectional feeding technology etc.In recent years, also there is a lot of patent application open for the improvement of upstriker riser reactor own, as CN1302843A discloses a kind of two sections of upstriker riser reactor catalytic cracking new technologies, the per pass conversion of raw material can be increased substantially, the product slates obtained.CN1633493A then discloses a kind of many upstrikers riser reactor technology, and CN1217366A then discloses a kind of multi-reaction-area upstriker riser reactor of producing in high-yield olefin, can significantly improve yield of light olefins.
Mix at downstriker riser reactor top with the catalyzer from revivifier at downstriker riser reactor Raw oil and along downstriker riser reactor cocurrent flow descending, under the oily effect at catalyzer of the process Raw of decline, cracking reaction occur.CN1603389A discloses a kind of two-part downstriker riser reactor catalyst cracking method and device, be mainly used in solving catalyzer existing for existing upstriker riser reactor and oil gas back-mixing serious, and degradation problem under the catalyzed reaction degree of reactor second half section existing for downstriker riser reactor technology.CN1530423A discloses a kind of catalytic cracking method for hydrocarbon oil of downstriker riser reactor, this reactor is injected by the feed nozzle making hydrocarbon oil crude material arrange through downstriker riser reactor plan vertical, the hydrocarbon oil crude material in atomizing state formed and catalyst exposure react, and are separated rapidly after downstriker riser reactor.The method can improve heavy oil conversion performance, obviously improve product slates.CN1546610A discloses a kind of catalytic cracking/cracking downstriker riser reactor processing heavy raw oil, devises the reactor of gas-solid cocurrent flow descending super short contact time catalysis.Patented invention application about the catalytic cracking technology of downstriker riser reactor openly also has a lot, can with reference to CN1552800A, CN1453334A, CN1530422A etc.
CN101210191A discloses the collapsible riser reactor catalyst cracking method that a kind of downstriker riser reactor is connected with upstriker riser reactor, stock oil after preheating enters downstriker riser reactor and contacts with the high-temperature regenerated catalyst from revivifier, gasify and carry out scission reaction, the oil gas exporting out from downstriker riser reactor enters upstriker riser reactor continuation reaction.This invention also according to the difference of target product, can adopt different catalyzer in two reactors.Adopt the method that this invention provides, can yield of gasoline be improved, improve quality product.
No matter above-mentioned patent is upstriker riser reactor, downstriker riser reactor or collapsible riser reactor, its oil gas and catalyzer are all to adopt and the mode flowed is advanced in the reactor, for heavy oil fluid catalytic cracking, this is more favourable, because heavy oil molecules is larger, be easy to be adsorbed on the surface of catalyzer and react, adopt cocurrent flow type can reduce the back-mixing of catalyzer, be convenient to control reaction depth, be conducive to the yield and the selectivity that improve the catalytic cracking process such as gasoline or diesel oil intermediate product.But, along with the development of refining & chemical industry integration, the dry gas adopting refinery to produce or light naphthar, or even hydrogen, ethene, the product such as propylene or butylene of the raw material production high added value such as Sweet natural gas, one of many oil refining enterprise main path of increasing economic efficiency, relative to traditional fluid catalytic cracking (FCC) technology, raw material and object product all have a very large change, and original riser reactor system cannot meet new requirement.These alkanes raw materials, its molecule is less, adsorptive power is more weak, during in existing riser reactor, also the mode of stream is reacted, when catalyst fluidization density is not high, raw molecule and catalyst active center's contact probability less, desirable reaction depth and object product selectivity cannot be reached.In addition, the green coke amount of this kind of reaction process is less, catalyst deactivation is not serious, and inactivation is comparatively slow, if adopt riser reactor, short period of time inner catalyst does not reach complete deactivation, catalyzer cannot be realized again stop for a long time in the reactor, catalyzer outflow reactor together with reaction oil gas of non-complete deactivation, can not again react with contact raw, thus it is not high to cause catalyst efficiency.
CN103360197A, although a kind of method disclosing fluidized-bed reactor counter current contact catalyzed conversion, the method mainly improves the productivity of propylene of C4-C8 conversion of olefines, and needs the intermediate pore molecular sieve catalyst coordinating particular modification.
Summary of the invention
In order to solve current refinery produce dry gas, light naphthar or the Sweet natural gas etc. that are rich in alkanes and carry out catalytic cracking, carrying out alkane conversion wherein that catalyzed conversion causes and the not high problem of selectivity of product when adopting traditional riser reactor, the invention provides following alkanes raw material and catalyzer being contacted in a fluidized bed reactor in a counter-current configuration and the method for catalytic conversion reaction and the technical scheme of conversion unit thereof occur:
A kind of alkanes catalysis conversion method, comprise alkanes raw material contact in a counter-current configuration in a fluidized bed reactor with catalyzer and the reactions steps of catalyzed conversion occurs, described alkanes raw material is one or more of the alkane of C1-C8, Sweet natural gas or light naphthar.
As the preferred version of above-mentioned alkanes catalysis conversion method, described catalyzed conversion carries out in fluidized reactor, alkanes raw material enters fluidized-bed reactor from fluidized-bed reactor bottom, described catalyzer is the regenerated catalyst from revivifier, regenerated catalyst enters fluidized-bed reactor from fluidized-bed reactor top, and up alkanes raw material and descending regenerated catalyst counter current contact react; Wherein, continue after the descending catalyst deactivation of described regenerated catalyst descendingly to enter stripper, after stripping, send into the regeneration of described revivifier, continue after regenerated catalyst catalyzed conversion that described alkanes raw material is passed through uply to enter the settlement separate a small amount of regenerated catalyst that it carries of settling vessel.
As the preferred version of above-mentioned alkanes catalysis conversion method, the described catalyzer residence time is in a fluidized bed reactor preferably 3s-30s.
As the preferred version of above-mentioned alkanes catalysis conversion method, described catalyzer is the particle that median size is preferably 60 μm-120 μm.
As the preferred version of above-mentioned alkanes catalysis conversion method, in described fluidized-bed reactor, the mixed oil and gas linear speed comprising alkanes raw material and catalyzed conversion product thereof is preferably between 0.1-1m/s.
As the preferred version of above-mentioned alkanes catalysis conversion method, described alkanes raw material is methane or Sweet natural gas, and described catalyzer is take aluminum oxide as the nickel catalyzator of carrier; Or described alkanes raw material is light naphthar, described catalyzer is ZSM-5 molecular sieve.
A kind of alkanes catalytic conversion reaction device, comprise fluidized-bed reactor 3, described fluidized-bed reactor 3 top is provided with catalyzer gatherer, fluidized-bed reactor 3 bottom is provided with alkanes raw material gatherer, wherein, the catalyzer take-up gear that one end that described fluidized-bed reactor 3 is provided with alkanes raw material gatherer is arranged is connected with stripper 5, the mixed oil and gas take-up gear of alkanes raw material after catalyzed conversion that one end that fluidized-bed reactor 3 is provided with catalyzer gatherer is arranged is connected with settling vessel 2, described catalyzer gatherer is connected with revivifier 12, and, settling vessel 2 bottom is connected with stripper 5, stripper 5 is connected by air-lift tube 10 with revivifier 12.
As the preferred version of above-mentioned hydrocarbons catalytic conversion reaction unit, described alkanes raw material gatherer is provided with multiple and highly different, and described catalyzer gatherer is provided with multiple and highly different.
As the preferred version of above-mentioned hydrocarbons catalytic conversion reaction unit, in the catalytic reaction zone of described fluidized-bed reactor 3, be provided with at least one in the expanding catalytic reaction zone of internal diameter or internal diameter undergauge catalytic reaction zone.
Adopt alkanes catalysis conversion method of the present invention, or adopt alkanes catalytic conversion reaction device of the present invention to carry out the catalytic conversion reaction of alkanes, the fluid density of catalyzer can be improved, increase the back-mixing of mixed oil and gas and catalyzer, improve mass transfer and heat transfer efficiency between mixed oil and gas and catalyzer, increase the contact probability of alkanes raw material and catalyst active center in mixed oil and gas, thus improve the transformation efficiency of alkanes raw material and the selectivity of object product.In addition, the catalyzer making inactivation not serious by alkanes raw material and catalyzer counter current contact flows downward and touches the active higher alkanes raw material of cracking reaction, keep catalyzed reaction continue efficiently carry out, improve the utilising efficiency of catalyzer; The mixed oil and gas simultaneously upwards flowed, although its cracking reaction activity declines to some extent, what touch is the regenerated catalyst that catalytic activity is higher, still can keep efficiently carrying out of catalyzed reaction, increase the reaction depth of alkanes raw material, improve yield and the selectivity of object product further.
Accompanying drawing explanation
Fig. 1 is alkanes catalytic conversion reaction apparatus structure schematic diagram of the present invention;
Mark in accompanying drawing and corresponding component names:
1-mixed oil and gas exports; 2-settling vessel; 3-fluidized-bed reactor; 4-alkanes material inlet; 5-stripper; 6-stripped vapor; 7-half spent agent valve; 8-spent agent valve; 9-gas lift air; 10-air-lift tube; 11-regeneration air; 12-revivifier; 13-exhanst gas outlet; 14-regenerator valve.
Embodiment
A kind of alkanes catalysis conversion method of the present invention, comprise alkanes raw material contact in a counter-current configuration in a fluidized bed reactor with catalyzer and the reactions steps of catalyzed conversion occurs, described alkanes raw material is one or more of the alkane of C1-C8, Sweet natural gas or light naphthar, be preferably Sweet natural gas, methane or light naphthar, wherein said light naphthar is the gasoline fraction of boiling range 20 DEG C ~ 70 DEG C.
In alkanes catalysis conversion method of the present invention, described catalyst type, can be different according to alkanes raw material, use corresponding various solid particle catalyst of the prior art, it is such as the nickel-base catalyst of carrier with aluminum oxide, ZSM-5 molecular sieve catalyzer take aluminum oxide as the molybdenum base alkane dehydrogenating catalyst etc. of carrier.Particularly when alkanes raw material is methane or Sweet natural gas, described catalyzer is that when taking aluminum oxide as the nickel catalyzator of carrier, methane conversion significantly improves; Described alkanes raw material is light naphthar, and when described catalyzer is ZSM-5 molecular sieve catalyzer, the yield of ethene and propylene and selectivity are obtained for and significantly improve.
In alkanes catalysis conversion method of the present invention, consider the reason that catalyzer dependence self gravitation flows downward, the median size of solid catalyst particle is preferably 30 μm-600 μm, more preferably 60 μm-120 μm.Described median size refers to according to laser particle size analyzer, the mean particle size obtained by the diffraction of particle or the spatial distribution of scattered light.
In alkanes catalysis conversion method of the present invention, described fluidized-bed reactor is not limited, alkanes raw material and catalyzer can be made can to contact in a counter-current configuration in the reactor and the setting reacted as long as comprise.Be preferably fluidized-bed reactor top and be provided with catalyzer gatherer, fluidized-bed reactor bottom is provided with alkanes raw material gatherer, step of reaction, described alkanes raw material enters fluidized-bed reactor from alkanes raw material gatherer, described catalyzer enters fluidized-bed reactor from catalyzer gatherer, and up alkanes raw material and descending catalyzer counter current contact react.Described fluidized-bed reactor can be the combination of one or more in dispersion fluidized bed, bubbling bed, turbulent bed or fast bed.
In alkanes catalysis conversion method of the present invention, because the few deactivation rate of alkanes raw material green coke amount is slower, adopt comparatively long residence time operation, the catalyzer of the present invention residence time is in a fluidized bed reactor 1s-3600s, consider the validity giving full play to catalyzer, the catalyzer residence time is in a fluidized bed reactor preferably 3s-30s.For the reasonable way of catalyzer of the present invention be cyclic regeneration use, such as above-mentioned top is provided with catalyzer gatherer, when bottom is provided with in the fluidized-bed reactor of alkanes raw material gatherer and carries out alkanes catalytic conversion reaction, continue after the descending catalyst deactivation of catalyzer descendingly to enter stripper, after stripping, send into the regeneration of described revivifier, the catalyzer after regeneration reenters fluidized-bed reactor through catalyzer gatherer and recycles.Catalyzer gatherer is provided with for above-mentioned top, when bottom is provided with in the fluidized-bed reactor of alkanes raw material gatherer and carries out alkanes catalytic conversion reaction, described alkanes raw material is passed through after being advanced into the settlement separate a small amount of regenerated catalyst that it carries of settling vessel on preferably continuing after regenerated catalyst catalyzed conversion and export from mixed oil and gas outlet, a small amount of regenerated catalyst be separated proceeds in described air stripper.
In alkanes catalysis conversion method of the present invention, due to employing is that boiling point is low, the small molecules alkanes raw material of easy gasification, and in the process of reaction, its green coke amount is less, the coke self generated possibly cannot meet the thermally equilibrated needs of whole device, so preferably adopt air and oil fuel and fuel gas to carry out regenerating in the regenerative process of described regenerated catalyst, air and oil fuel carry out regenerating or air and fuel gas regenerate, thus better can maintain the heat required for whole device.Also can with riser fluid catalytic cracking conbined usage on applicable industry, share a revivifier, the feature of heat surplus in positive good utilisation heavy-oil catalytic, carry out the problem that supplementary light paraffins class reacts self heat supply deficiency in a fluidized bed reactor, but also the temperature of regenerator in Catalytic Unit can be reduced by this method, thus improve the agent-oil ratio of heavy-oil catalytic, improve its products distribution, economy system is invested, and saves running cost, achieves many things at one stroke.
In alkanes catalysis conversion method of the present invention, the mixed oil and gas linear speed in fluidized-bed reactor is compared with riser catalytic cracking technology, slightly little, and is advisable with speed when reaching conveying bed lower than particle, adopts 0.01-5m/s, is preferably 0.1-1m/s.
In alkanes catalysis conversion method of the present invention, alkanes raw material and catalyzer contact in a counter-current configuration in a fluidized bed reactor and occur catalyzed conversion temperature of reaction control be 400 ~ 1000 DEG C, its preferable reaction temperature is 600 ~ 800 DEG C.
Below in conjunction with accompanying drawing, a kind of alkanes catalytic conversion reaction equipment provided by the present invention is further illustrated, but the present invention is not limited to the alkanes catalytic conversion reaction device shown in Fig. 1: as shown in Figure 1, alkanes catalytic conversion reaction device of the present invention, comprise fluidized-bed reactor 3, described fluidized-bed reactor 3 top is provided with catalyzer gatherer, fluidized-bed reactor 3 bottom is provided with alkanes raw material gatherer, wherein, the catalyzer take-up gear that one end that described fluidized-bed reactor 3 is provided with alkanes raw material gatherer is arranged is connected with stripper 5, the mixed oil and gas take-up gear that one end that fluidized-bed reactor 3 is provided with catalyzer gatherer is arranged is connected with settling vessel 2, described catalyzer gatherer is connected with revivifier 12, and, settling vessel 2 bottom is connected with stripper 5, stripper 5 is connected by air-lift tube 10 with revivifier 12.In order to better control importing or the transfer of catalyzer, regenerator valve 14 is provided with between catalyzer gatherer and revivifier 12, be connected with half spent agent valve 7 between settling vessel 2 bottom and stripper 5, between stripper 5 and air-lift tube 10, be provided with spent agent valve 8.
In alkanes catalytic conversion reaction equipment of the present invention, for avoiding the harmful competition between different alkanes raw material, according to the parameter such as temperature and level of deactivation of feedstock property, catalyzer, can multiple alkanes raw material gatherer be set on the bottom different heights of fluidized-bed reactor 3, make alkanes raw material of different nature enter fluidized-bed reactor at the different positions of fluidized-bed reactor, thus per share alkanes raw material is reacted all as much as possible under optimal condition.In order to increase the flexibility of operation of conversion unit, multiple catalyzer gatherer can be set at the different heights place, top of fluidized-bed reactor, thus the thermograde formed from top to bottom and catalyst activity gradient, increase the control to differential responses region, improve object product yield and selectivity.
In alkanes catalytic conversion reaction equipment of the present invention, in order to meet the needs to the different fluid density of catalyzer of alkanes raw material in fluidized-bed reactor, the way of expanding catalytic reaction zone and/or undergauge catalytic reaction zone can be adopted on the different heights of fluidized-bed reactor, carry out mixed oil and gas linear speed in altering reactor, thus change the fluidized state of catalyzer, change the fluid density of catalyzer.
In alkanes catalytic conversion reaction equipment of the present invention, in order to prevent occurring the fluidized states such as large bubble coalescence, channel or joint gush in a fluidized bed reactor, redistributor can be set at fluidized-bed reactor inner different positions, comprise orifice plate, grid and/or chev(e)ron baffle etc.By the rectification of redistributor, make the flow state of mixed oil and gas and catalyzer more even, degree of mixing is more desirable.
In alkanes catalytic conversion reaction equipment of the present invention, alkanes catalytic conversion reaction equipment of the present invention can with riser fluid catalytic cracking conbined usage on applicable industry, share a revivifier.Thus the feature of Catalytic Unit heat surplus can be utilized, carry out the problem that supplementary light paraffins class raw material reacts self heat supply deficiency in a fluidized bed reactor, but also the temperature of regenerator in Catalytic Unit can be reduced by this method, thus improve the agent-oil ratio of heavy-oil catalytic, improve its products distribution.Can also invest by economy system simultaneously, save running cost.
Embodiment
Embodiment 1
Take ZSM-5 molecular sieve as catalyzer median size it is 80 μm, light naphthar (gasoline fractions that boiling range is 20 DEG C ~ 70 DEG C) is alkanes raw material, catalytic conversion reaction is carried out in alkanes catalytic conversion reaction equipment as shown in Figure 1, fluidized-bed reactor internal diameter is 50mm, be highly 3000mm, using the overheated steam of 500 DEG C as stripping fluid, take air as regenerating medium, the regeneration temperature of catalyzer controls at 700 DEG C, in fluidized-bed reactor, after oil gas and catalyst exposure, finish mixing temperature controls at about 600 DEG C, the speed that regenerated catalyst imports fluidized-bed reactor is 20 kgs/hour, mixed oil and gas linear speed in fluidized-bed reactor controls at 0.8m/s, the mixed oil and gas residence time controls at 3s.
Comparative example 1
Take ZSM-5 molecular sieve as catalyzer median size 80 μm, light naphthar (gasoline fractions that boiling range is 20 DEG C ~ 70 DEG C) is alkanes raw material, catalytic conversion reaction is carried out in conventional lift pipe catalytic cracking unit, riser reactor internal diameter is 16mm, be highly 3000mm, using the overheated steam of 500 DEG C as stripping fluid, take air as regenerating medium, the regeneration temperature of catalyzer controls at 700 DEG C, riser reactor middle outlet temperature controls at about 600 DEG C, the speed that regenerated catalyst imports riser reactor is 20 kgs/hour, mixed oil and gas linear speed in riser reactor controls at 8m/s, about the 3s that the mixed oil and gas residence time controls.
Embodiment 1 the results are shown in subordinate list 1 with comparative example 1.Result from subordinate list 1, compared with the catalytic cracking in riser reactor, the transformation efficiency that light naphthar reacts with catalyzer counter current contact is in a fluidized bed reactor higher, 3.34 percentage points are exceeded, particularly crucially the yield of object product ethene and propylene improves 0.49 and 3.46 percentage point respectively, sum of the two is also larger than the amplification of transformation efficiency, illustrate that alkanes raw material and the reaction of catalyzer counter current contact improve the selectivity of object product in a fluidized bed reactor: the concentration of ethene in dry gas has brought up to 85.51% by 75.46%, the concentration of propylene in liquefied gas has then brought up to 61.20% by 58.69%.Experimental result shows, compared with the catalytic cracking in riser reactor, after petroleum naphtha reacts with catalyzer counter current contact in a fluidized bed reactor, yield and the selectivity of ethene and propylene are obtained for raising.
Subordinate list 1: the contrast reaction result of petroleum naphtha in fluidized-bed reactor and riser reactor
Embodiment 2
Take nickel as active ingredient, aluminum oxide is the methane catalytic decomposition catalyst for preparing hydrogen of carrier, median size is 100 μm, methane is alkanes raw material, catalytic conversion reaction is carried out in alkanes catalytic conversion reaction equipment as shown in Figure 1, fluidized-bed reactor internal diameter is 50mm, be highly 3000mm, the overheated steam of 500 DEG C is as stripping fluid, take air as regenerating medium, the regeneration temperature of catalyzer controls at 780 DEG C, finish mixing temperature in fluidized-bed reactor after oil gas and catalyst exposure controls at about 700 DEG C, the speed that regenerated catalyst imports fluidized-bed reactor is 30 kgs/hour, the mixed oil and gas linear speed of fluidized-bed reactor controls at 1.5m/s, the mixed oil and gas residence time controls at 10s.
Comparative example 2
Take nickel as active ingredient, aluminum oxide is the methane catalytic decomposition catalyst for preparing hydrogen of carrier, median size is 100 μm, methane is alkanes raw material, catalytic conversion reaction is carried out in conventional lift pipe catalytic cracking unit, riser reactor internal diameter is 16mm, be highly 3000mm, using the overheated steam of 500 DEG C as stripping fluid, take air as regenerating medium, the regeneration temperature of catalyzer controls at 780 DEG C, riser reactor middle outlet temperature controls at about 700 DEG C, the speed that regenerated catalyst imports riser reactor is 30 kgs/hour, mixed oil and gas linear speed in riser reactor controls at 8m/s, about the 3s that the mixed oil and gas residence time controls.
Embodiment 2 the results are shown in subordinate list 2 with comparative example 2.The primary product of methane catalytic decomposition is hydrogen and deposition coke on a catalyst, additional a small amount of water, carbon monoxide and carbonic acid gas.Result as can be seen from subordinate list 2, compared with traditional riser fluid catalytic cracking, the methane transformation efficiency that methane and catalyzer counter current contact are reacted in a fluidized bed reactor significantly improves, and has exceeded 17.29 percentage points, both hydrogen selectives are suitable, are all greater than 97%.
Subordinate list 2: the contrast reaction result of methane in fluidized-bed reactor and riser reactor
| Methane conversion wt% | *Hydrogen selective % | |
| Embodiment 2 | 92.12 | 97.58 |
| Comparative example 2 | 74.83 | 97.63 |
*hydrogen selective refers to that the actual product hydrogen quality of every 100g methane after catalyzed conversion produces hydrogen mass ratio with theoretical.
Claims (10)
1. an alkanes catalysis conversion method, it is characterized in that, comprise alkanes raw material contact in a counter-current configuration in a fluidized bed reactor with catalyzer and the reactions steps of catalyzed conversion occurs, described alkanes raw material is one or more of the alkane of C1-C8, Sweet natural gas or light naphthar.
2. alkanes catalysis conversion method according to claim 1, it is characterized in that described catalyzed conversion carries out in fluidized reactor, alkanes raw material enters fluidized-bed reactor from fluidized-bed reactor bottom, described catalyzer is the regenerated catalyst from revivifier, regenerated catalyst enters fluidized-bed reactor from fluidized-bed reactor top, and up alkanes raw material and descending regenerated catalyst counter current contact react; Wherein, continue after the descending catalyst deactivation of described regenerated catalyst descendingly to enter stripper, after stripping, send into the regeneration of described revivifier, continue after regenerated catalyst catalyzed conversion that described alkanes raw material is passed through uply to enter the settlement separate a small amount of regenerated catalyst that it carries of settling vessel.
3. alkanes catalysis conversion method according to claim 1, is characterized in that the described catalyzer residence time is in a fluidized bed reactor 3s-30s.
4. alkanes catalysis conversion method according to claim 7, is characterized in that described catalyzer is the particle of median size 60 μm-120 μm.
5. alkanes catalysis conversion method according to claim 1, is characterized in that described oil gas linear speed is between 0.1-1m/s.
6. alkanes catalysis conversion method according to claim 1, is characterized in that described alkanes raw material is methane or Sweet natural gas, and described catalyzer is take aluminum oxide as the nickel catalyzator of carrier.
7. alkanes catalysis conversion method according to claim 1, it is characterized in that described alkanes raw material is light naphthar, described catalyzer is ZSM-5 molecular sieve.
8. an alkanes catalytic conversion reaction device, comprise fluidized-bed reactor (3), described fluidized-bed reactor (3) top is provided with catalyzer gatherer, fluidized-bed reactor (3) bottom is provided with alkanes raw material gatherer, it is characterized in that the catalyzer take-up gear that one end that described fluidized-bed reactor (3) is provided with alkanes raw material gatherer is arranged is connected with stripper (5), the mixed oil and gas take-up gear of alkanes raw material after catalyzed conversion that one end that fluidized-bed reactor (3) is provided with catalyzer gatherer is arranged is connected with settling vessel (2), described catalyzer gatherer is connected with revivifier (12), and, settling vessel (2) bottom is connected with stripper (5), stripper (5) is connected by air-lift tube (10) with revivifier (12).
9. alkanes catalytic conversion reaction device according to claim 8, is characterized in that described alkanes raw material gatherer is provided with multiple and highly different, and described catalyzer gatherer is provided with multiple and highly different.
10. alkanes catalytic conversion reaction device according to claim 8, is provided with at least one in the expanding catalytic reaction zone of internal diameter or internal diameter undergauge catalytic reaction zone in the catalytic reaction zone that it is characterized in that described fluidized-bed reactor (3).
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| CN109107615A (en) * | 2017-06-23 | 2019-01-01 | 中国石油大学(华东) | A kind of alkane dehydrogenating catalyst regeneration method and regenerating unit |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104069779A (en) * | 2013-03-27 | 2014-10-01 | 中国石油天然气集团公司 | Fluidized bed reaction device for olefin production by alkane dehydrogenation and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104069779A (en) * | 2013-03-27 | 2014-10-01 | 中国石油天然气集团公司 | Fluidized bed reaction device for olefin production by alkane dehydrogenation and method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109107615A (en) * | 2017-06-23 | 2019-01-01 | 中国石油大学(华东) | A kind of alkane dehydrogenating catalyst regeneration method and regenerating unit |
| CN109107615B (en) * | 2017-06-23 | 2021-07-09 | 中国石油大学(华东) | Regeneration method and regeneration device for alkane dehydrogenation catalyst |
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Application publication date: 20150902 |