CN101293803A - Method for converting oxygen-containing compounds into low carbon olefin hydrocarbon - Google Patents
Method for converting oxygen-containing compounds into low carbon olefin hydrocarbon Download PDFInfo
- Publication number
- CN101293803A CN101293803A CNA2008101083561A CN200810108356A CN101293803A CN 101293803 A CN101293803 A CN 101293803A CN A2008101083561 A CNA2008101083561 A CN A2008101083561A CN 200810108356 A CN200810108356 A CN 200810108356A CN 101293803 A CN101293803 A CN 101293803A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- low
- sapo
- carbon alkene
- weight
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a method for converting oxygen-containing compound into low-carbon olefin mainly for solving the problem in the prior art of low yield of the low-carbon olefin. The method is characterized in that regenerated catalyst is returned to a stripping region via a catalyst riser; and the stripping region is used as a catalyst mixing region. The method can be applied to the industrial production of the low-carbon olefin.
Description
Technical field
The present invention relates to the method that a kind of oxygenate is a low-carbon alkene.
Technical background
Low-carbon alkene, promptly ethene and propylene are 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 because limited supply of petroleum resources and higher price, the cost of being produced ethene, propylene by petroleum resources constantly increases.In recent years, people begin to greatly develop the technology that alternative materials transforms system ethene, propylene.Wherein, the alternative materials that is used for light olefin production that one class is important is an oxygenatedchemicals, for example 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 technology is very ripe, can realize up to a million tonnes industrial scale.Because the popularity in oxygenatedchemicals source is added and is transformed the economy that generates light olefin technology, so by the technology of oxygen-containing compound conversion to produce olefine (OTO), particularly the technology by methanol conversion system alkene (MTO) is subjected to increasing attention.
In the US4499327 patent silicoaluminophosphamolecular molecular sieves catalyzer is applied to methanol conversion system olefin process and studies in great detail, think that SAPO-34 is the first-selected catalyzer of MTO technology.The SAPO-34 catalyzer has very high light olefin selectivity, and activity is also higher, and can make methanol conversion is the degree that was less than in reaction times of light olefin 10 seconds, more even reach in the reaction time range of riser tube.
Announced among the US6166282 that a kind of oxygenate conversion is the technology and the reactor of low-carbon alkene, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu reaction of gas speed is finished, after rising to the fast subregion that internal diameter diminishes rapidly, adopt special gas-solid separation equipment initial gross separation to go out most entrained catalyst.Because reaction after product gas and catalyzer sharp separation have 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 significantly reduce.
Announced among the CN1723262 that it is low-carbon alkene technology that the multiple riser reaction unit that has central catalyst return is used 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 product gas are separated.
Known in the field, guarantee high selectivity of light olefin, need the carbon distribution of some amount on the catalyzer, and oxygenate is very responsive to processing parameters such as temperature of reaction in the process of low-carbon alkene.All there are problems such as the fluctuation of reaction zone inner catalyst carbon deposit skewness, temperature of reaction is big in prior art.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 selectivity of light olefin that exists in the prior art, and it is the method for low-carbon alkene that a kind of new oxygenate is provided.This method is used for the production of low-carbon alkene, has that selectivity of light olefin is higher, low-carbon alkene production technique economy advantage of higher.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of oxygenate is the method for low-carbon alkene, said method comprising the steps of: a kind of fluidized-bed reactor (a) is provided, comprise reaction zone, race way, stripping zone, disengaging zone, the raw material that comprises described oxygenatedchemicals is contacted under the condition for validity of described reaction zone with comprising the silicoaluminophosphamolecular molecular sieve catalyzer, form the logistics 1 that comprises low-carbon alkene, catalyzer; (b) catalyzer in the described logistics 1 is separated in the disengaging zone, forms reclaimable catalyst, and described reclaimable catalyst enters stripping zone; (c) will be divided into two portions at least through steam stripped described reclaimable catalyst, wherein first part turns back to the bottom of described reaction zone by the catalyst transport pipeline, wherein second section enters revivifier by the catalyst transport pipeline and contacts the formation regenerated catalyst with regenerating medium; (d) at least a portion of described regenerated catalyst enters in the catalyst transport standpipe, contact with the lifting medium, the regenerated catalyst of described at least a portion is thus lifted to the disengaging zone of described reactor, after the gas-solid cyclone separator separation, the regenerated catalyst of described at least a portion enters stripping zone, mixes with described reclaimable catalyst.
In the technique scheme, described oxygen-containing compound material is selected from least a in methyl alcohol, the dme, and preferred version is selected from methyl alcohol; Silicoaluminophosphamolecular molecular sieve is selected from least a among SAPO-5, SAPO-11, SAPO-17, SAPO-18, SAPO-34, SAPO-35, SAPO-44 or the SAPO-56, and preferred version is selected from SAPO-34; Described reactor is fast fluidized bed or riser tube, and preferred version is selected from fast fluidized bed; Stripping medium in the described stripping zone is a water vapour; Lifting medium in the described catalyst transport standpipe is at least a in oxygenatedchemicals, water vapour or the reactor product that comprises methyl alcohol, dme, preferred version is to be selected from the above hydrocarbon of oxygenatedchemicals, water vapour or C4 that comprises methyl alcohol, dme, and more preferably scheme is for being selected from the above hydrocarbon of C4; Described first part catalyzer is through returning the reaction zone bottom after the heat exchange, heat transferring medium is a water vapour; Described condition for validity is: reaction pressure is counted 0～1MPa with gauge pressure, and temperature of reaction is 300～600 ℃, and the raw material weight hourly space velocity is 1～50 hour
-1, the average coke content of reaction zone catalyzer is 0.01～7% weight, and the described condition for validity of preferred version is: reaction pressure is counted 0.01～0.3MPa with gauge pressure, and temperature of reaction is 400～500 ℃, and the raw material weight hourly space velocity is 6～25 hours
-1, the average coke content of reaction zone catalyzer is 1～4% weight; The reclaimable catalyst that described second section enters revivifier by the catalyst transport pipeline accounts for 5～90% weight of total reclaimable catalyst, and preferred version is 15～40% weight; 10～100% weight of described regenerated catalyst enter in the catalyst transport standpipe, contact with promoting medium, and preferred version is selected from 50～100% weight.
Weight hourly space velocity of the present invention is defined as the raw material inlet amount that comprises in unit time active ingredient (as the molecular sieve) content divided by the reaction zone inner catalyst.
Carbon deposit quality on the catalyzer that coke content method of calculation of the present invention are certain mass is divided by described catalyst quality.Carbon deposit measuring method on the catalyzer is as follows: will mix the catalyst mix that has carbon deposit that comparatively all has, the accurate carbon-bearing catalyzer of weighing certain mass then, be put in the pyrocarbon analyser and burn, the carbonic acid gas quality that generates by infrared analysis burning, thus carbonaceous amount on the catalyzer obtained.
The all right non-imposed common charging of a certain proportion of thinner of interpolation in reactor feed, thinner can be low-carbon alkanes (methane, ethane), CO, nitrogen, water vapour, C4 hydrocarbon, mononuclear aromatics etc., wherein, preferred low-carbon alkanes, water vapour, most preferably scheme is a water vapour, and the amount of thinner and the volume ratio of raw material are 0.1～10: regulate in 1 scope.
Because oxygenate is in the reaction process of low-carbon alkene, needs to be with on the catalyzer a certain amount of carbon, to improve the selectivity of low-carbon alkene.General, adopt with reclaimable catalyst and regenerated catalyst blended method, to reach required coke content requirement.And more importantly be that before mixed catalyst contact raw material, catalyzer requires to mix, and could realize maximized selectivity requirement.Known in the field, in the existing circulating fluidized bed technique, as fluid catalytic cracking (FCC), be regenerated catalyst directly to be turned back to riser reaction zone contact with raw material, but, do not relate to the mixed problem of different carbon-bearing amount catalyzer because prior art generally all requires the mean carbon content of reaction zone catalyzer low more good more.In addition, because oxygenate is that the reaction of low-carbon alkene is very responsive for temperature of reaction, the fluctuation of reaction zone temperature of reaction will directly influence reaction effect, if the higher regenerated catalyst of temperature directly turns back to reaction zone, will certainly influence the temperature of reaction of reaction zone.Therefore, generally speaking, be in the process of low-carbon alkene in oxygenate, the solid flow of regenerated catalyst line mainly plays two effects: the one, control suitable flow and mix with reclaimable catalyst, reach the required average coke content of catalyzer; The 2nd, control suitable flow and enter reaction zone, guarantee the stable of heat that reaction zone is required and temperature of reaction.And in the prior art, above-mentioned two effects tend to produce contradiction, as: the regenerated catalyst flow is big, the heat height that obtains of reaction zone then, temperature of reaction raises, but owing to the ratio of regenerated catalyst in the mixed catalyst increases, has then reduced the average coke content of mixed catalyst.Adopt method of the present invention, regenerated catalyst is turned back to stripping zone by the catalyzer standpipe, and, reduced the temperature of regenerated catalyst simultaneously, effectively solved the problems referred to above the mixing region of stripping zone as catalyzer.In addition, method of the present invention has also reduced the height of revivifier to a certain extent.
Adopt method of the present invention, regenerated catalyst risen to the disengaging zone of reactor by promoting medium so that and reclaimable catalyst mix, can also reach the effect that influences the reaction zone operating parameters that minimizes.In addition, because methyl alcohol or dimethyl ether conversion are in the reaction process of low-carbon alkene, can there be unreacted methanol or dme, and can produce the above hydrocarbon of the lower C4 of a certain amount of added value, if the above hydrocarbon of C4 in unreacted methanol or dme or the product is contacted with regenerated catalyst as promoting medium, not only can generate low-carbon alkene, improved the utilising efficiency of methyl alcohol or dme or the above hydrocarbon of C4, but also regenerated catalyst has been carried out pre-coking, thereby the carbon that dwindles reclaimable catalyst and regenerated catalyst is poor.When the average coke content one of reaction zone mixed catalyst regularly because the carbon difference of reclaimable catalyst and regenerated catalyst is less, catalyst carbon deposit narrow distribution then, thereby improved the selectivity of low-carbon alkene greatly.In addition, because dwindling of reclaimable catalyst and regenerated catalyst carbon difference can be adopted bigger catalyst recirculation amount operation between reaction and regeneration system rapidly, be easy to control more.
Adopt technical scheme of the present invention: described oxygen-containing compound material is selected from least a in methyl alcohol, the dme; Silicoaluminophosphamolecular molecular sieve is selected from least a among SAPO-5, SAPO-11, SAPO-17, SAPO-18, SAPO-34, SAPO-35, SAPO-44 or the SAPO-56; Described reactor is fast fluidized bed or riser tube; Stripping medium in the described stripping zone is a water vapour; Lifting medium in the described catalyst transport standpipe is the above hydrocarbon of oxygenatedchemicals, water vapour or C4 that comprises methyl alcohol, dme; Described first part catalyzer is through returning the reaction zone bottom after the heat exchange, heat transferring medium is a water vapour; Described condition for validity is: reaction pressure is counted 0～1MPa with gauge pressure, and temperature of reaction is 300～600 ℃, and the raw material weight hourly space velocity is 1～50 hour
-1, the average coke content of reaction zone catalyzer is 0.01～7% weight; The reclaimable catalyst that described second section enters revivifier by the catalyst transport pipeline accounts for 5～90% weight of total reclaimable catalyst, 10～100% weight of described regenerated catalyst enter in the catalyst transport standpipe, contact with the lifting medium, selectivity of light olefin can reach 85.26% weight, has obtained better technical effect.
Description of drawings
Fig. 1 is the schematic flow sheet of the method for the invention.
Among Fig. 1,1 is the reactor feedstocks charging; 2 is reactor reaction zone; 3 are gas-solid sharp separation equipment; 4 is stripping zone; 5 is reclaimable catalyst circulation inclined tube; 6 remove the revivifier line of pipes for reclaimable catalyst; 7 is interchanger; 8 is the reactor gas-solid cyclone separator; 9 is the reactor disengaging zone; 10 is the product collection chamber; 11 is the product gas outlet pipeline; 12 is revivifier; 13 is the regenerating medium source line; 14 is the revivifier breeding blanket; 15 is the revivifier external warmer; 16 is the revivifier gas-solid cyclone separator; 17 is the regenerated flue gas outlet line; 18 is the regenerated catalyst line; 19 are regenerated catalyst standpipe lifting medium inlet pipeline; 20 is the mixing section of regenerated catalyst standpipe bottom; 21 is regenerated catalyst standpipe; 22 gas-solid cyclone separators for the regenerated catalyst standpipe outlet.
Oxygen-containing compound material enters in the reactor reaction zone 2 through feeding line 1, contact with molecular sieve catalyst, reaction generates the product that contains low-carbon alkene, carry reclaimable catalyst and enter the reactor Disengagement zone through the quick separation equipment 3 of gas-solid, wherein, most of catalyst that the quick separation equipment 3 of gas-solid is separated enters stripping zone 4, and gaseous products and part are not carried out Re-isolation by the catalyst that the quick separation equipment of gas-solid separates through entering cyclone separator 8 separation, catalyst turns back to stripping zone 4 through the dipleg of cyclone separator 8, and gaseous products enters collection chamber 10 and enters follow-up centrifugal station by outlet line 11. Be divided into two parts by the quick separation equipment 3 of gas-solid and cyclone separator 8 isolated reclaimable catalysts through behind the stripping, turn back to the bottom of reaction zone 2 after 7 heat exchange of part process heat exchanger by catalyst circulation inclined tube 5, a part enters coke-burning regeneration in the renewing zone 14 of regenerator 12 through catalyst transport pipeline 6 in addition, the flue gas that the coke burning generates enters follow-up energy-recuperation system through behind the cyclone separator 16 by exhanst gas outlet pipeline 17, the catalyst that regeneration is finished enters in the mixing section 20 of catalyst standpipe 21 bottoms by catalyst transport pipeline 18, mix with lifting medium 19, regenerated catalyst is promoted in the reactor Disengagement zone 9, the regenerated catalyst standpipe outlet is provided with gas-solid cyclone separator 22, isolated regenerated catalyst enters in the stripping zone 4 and mixes with reclaimable catalyst, and part turns back to sustainable participation reaction in the reaction zone 2 through circulation inclined tube 5.
The invention will be further elaborated below by embodiment, but be not limited only to present embodiment.
Embodiment
[embodiment 1～4]
In small-sized fast fluidized bed reaction unit, the same Fig. 1 of reactor pattern.The reaction zone medial temperature is 500 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, pure methanol feeding, and the methyl alcohol weight hourly space velocity is 25 hours
-1, catalyst type sees Table 1, and stripping zone stripping medium is a water vapour, and it is water vapour that regenerated catalyst standpipe promotes medium, and the heat transferring medium with reclaimable catalyst in the interchanger 7 is a water vapour.The reclaimable catalyst that second section enters revivifier 12 by catalyst transport pipeline 6 accounts for 40% weight of total reclaimable catalyst, 100% weight of described regenerated catalyst enters in the catalyst transport standpipe, contact with promoting medium, the average coke content of the catalyzer in the reaction zone 2 is 2.5% weight.Keep the stability of catalyst flow control, the reactor outlet product adopts online gas chromatographic analysis, and experimental result sees Table 1.
Table 1
| Parameter | Catalyst type | Low-carbon alkene carbon back selectivity, % weight |
| Embodiment 1 | SAPO-11 | 33.13 |
| Embodiment 2 | SAPO-18 | 78.33 |
| Embodiment 3 | SAPO-56 | 49.43 |
| Embodiment 4 | SAPO-34 | 80.12 |
[embodiment 5～6]
According to [embodiment 4] described condition, just change temperature of reactor, experimental result sees Table 2.
Table 2
| Parameter | Temperature of reaction, ℃ | Low-carbon alkene carbon back selectivity, % weight |
| Embodiment 5 | 400 | 75.95 |
| Embodiment 6 | 450 | 81.17 |
[embodiment 7～8]
According to [embodiment 4] described condition, just change type of feed and raw material weight hourly space velocity, experimental result sees Table 3.
Table 3
| Parameter | Type of feed | Raw material weight hourly space velocity hour -1 | Low-carbon alkene carbon back selectivity % weight |
| Embodiment 7 | Dme | 15 | 78.91 |
| Embodiment 8 | Methyl alcohol: dme=5: 1 | 6 | 79.87 |
[embodiment 9～11]
According to [embodiment 4] described condition, change reactor pattern, reaction pressure and raw material weight hourly space velocity, experimental result sees Table 4.
Table 4
| Parameter | The reactor pattern | Raw material weight hourly space velocity hour -1 | Reaction pressure is in gauge pressure MPa | Low-carbon alkene carbon back selectivity % weight |
| Embodiment 9 | Riser tube | 50 | 0.3 | 76.69 |
| Embodiment 10 | Fast fluidized bed | 1.2 | 0.01 | 78.28 |
| Embodiment 11 | Fast fluidized bed | 50 | 1.0 | 74.57 |
[embodiment 12～14]
According to [embodiment 4] described condition, change ratio and average coke content that reclaimable catalyst that second section enters revivifier 12 by catalyst transport pipeline 6 accounts for total reclaimable catalyst, 50% weight of described regenerated catalyst enters in the catalyst transport standpipe, contact with promoting medium, experimental result sees Table 5.
Table 5
| Parameter | The average coke content of reaction zone catalyzer, % weight | The reclaimable catalyst weight that second section enters revivifier accounts for the ratio of total reclaimable catalyst weight, % | Low-carbon alkene carbon back selectivity, % weight |
| Embodiment 12 | 1.0 | 15 | 73.85 |
| Embodiment 13 | 4.0 | 60 | 76.44 |
| Embodiment 14 | 7.0 | 5 | 74.12 |
[comparative example 1]
According to [embodiment 4] described condition, just regenerated catalyst is directly turned back to reaction zone 2 bottoms, low-carbon alkene carbon back selectivity is 78.15% weight.
[comparative example 2]
According to [embodiment 13] described condition, regenerated catalyst is directly turned back to reaction zone 2 bottoms, low-carbon alkene carbon back selectivity is 74.99% weight.
[embodiment 15～16]
In small-sized fast fluidized bed reaction unit, the same Fig. 1 of reactor pattern.The reaction zone medial temperature is 500 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, pure methanol feeding, and the methyl alcohol weight hourly space velocity is 25 hours
-1, catalyst type sees Table 6, and stripping zone stripping medium is a water vapour, and it is unreacted methanol and dme that regenerated catalyst standpipe promotes medium, and the heat transferring medium with reclaimable catalyst in the interchanger 7 is a water vapour.The reclaimable catalyst that second section enters revivifier 12 by catalyst transport pipeline 6 accounts for 50% weight of total reclaimable catalyst, 100% weight of described regenerated catalyst enters in the catalyst transport standpipe, contact with promoting medium, the average coke content of the catalyzer in the reaction zone 2 is 2.5% weight.Keep the stability of catalyst flow control, the reactor outlet product adopts online gas chromatographic analysis, and experimental result sees Table 6.
Table 6
| Parameter | Catalyst type | Low-carbon alkene carbon back selectivity, % weight |
| Embodiment 15 | SAPO-18 | 79.54 |
| Embodiment 16 | SAPO-34 | 82.78 |
[embodiment 17～18]
According to [embodiment 16] described condition, it is the above hydrocarbon of the isolated C4 of product separation workshop section that regenerated catalyst standpipe promotes medium, changes temperature of reactor, and experimental result sees Table 7.
Table 7
| Parameter | Temperature of reaction, ℃ | Low-carbon alkene carbon back selectivity, % weight |
| Embodiment 3 | 400 | 79.10 |
| Embodiment 4 | 450 | 85.26 |
[embodiment 19～20]
According to [embodiment 18] described condition, just change type of feed and raw material weight hourly space velocity, experimental result sees Table 8.
Table 8
| Parameter | Type of feed | Raw material weight hourly space velocity hour -1 | Low-carbon alkene carbon back selectivity % weight |
| Embodiment 19 | Dme | 15 | 84.23 |
| Embodiment 20 | Methyl alcohol: dme=5: 1 | 6 | 85.09 |
[embodiment 21～23]
According to [embodiment 18] described condition, change reactor pattern, reaction pressure and raw material weight hourly space velocity, experimental result sees Table 9.
Table 9
| Parameter | The reactor pattern | Raw material weight hourly space velocity hour -1 | Reaction pressure is in gauge pressure MPa | Low-carbon alkene carbon back selectivity % weight |
| Embodiment 21 | Riser tube | 50 | 0.3 | 79.99 |
| Embodiment 22 | Fast fluidized bed | 1.2 | 0.01 | 81.24 |
| Embodiment 23 | Fast fluidized bed | 50 | 1.0 | 76.11 |
[embodiment 24～26]
According to [embodiment 16] described condition, change ratio and average coke content that reclaimable catalyst that second section enters revivifier 12 by catalyst transport pipeline 6 accounts for total reclaimable catalyst, 50% weight of described regenerated catalyst enters in the catalyst transport standpipe, contact with promoting medium, experimental result sees Table 10.
Table 10
| Parameter | The average coke content of reaction zone catalyzer, % weight | The reclaimable catalyst weight that second section enters revivifier accounts for the ratio of total reclaimable catalyst weight, % | Low-carbon alkene carbon back selectivity, % weight |
| Embodiment 24 | 1.0 | 20 | 76.46 |
| Embodiment 25 | 4.0 | 70 | 78.21 |
| Embodiment 26 | 7.0 | 5 | 76.90 |
[comparative example 3]
According to [embodiment 16] described condition, just regenerated catalyst is directly turned back to reaction zone 2 bottoms, low-carbon alkene carbon back selectivity is 79.86% weight.
[comparative example 4]
According to [embodiment 25] described condition, regenerated catalyst is directly turned back to reaction zone 2 bottoms, low-carbon alkene carbon back selectivity is 76.31% weight.
Obviously, adopt method of the present invention, can reach the purpose that improves selectivity of light olefin, have bigger technical superiority, can be used in the industrial production of low-carbon alkene.
Claims (10)
1, a kind of oxygenate is the method for low-carbon alkene, said method comprising the steps of:
(a) provide a kind of fluidized-bed reactor, comprise reaction zone, race way, stripping zone, disengaging zone, the raw material that comprises described oxygenatedchemicals is contacted under the condition for validity of described reaction zone with comprising the silicoaluminophosphamolecular molecular sieve catalyzer, form the logistics 1 that comprises low-carbon alkene, catalyzer;
(b) catalyzer in the described logistics 1 is separated in the disengaging zone, forms reclaimable catalyst, and described reclaimable catalyst enters stripping zone;
(c) will be divided into two portions through steam stripped described reclaimable catalyst, wherein first part turns back to the bottom of described reaction zone by the catalyst transport pipeline, wherein second section enters revivifier by the catalyst transport pipeline and contacts the formation regenerated catalyst with regenerating medium;
(d) at least a portion of described regenerated catalyst enters in the catalyst transport standpipe, contact with the lifting medium, the regenerated catalyst of described at least a portion is thus lifted to the disengaging zone of described reactor, after the gas-solid cyclone separator separation, the regenerated catalyst of described at least a portion enters stripping zone, mixes with described reclaimable catalyst.
2, be the method for low-carbon alkene according to the described oxygenate of claim 1, it is characterized in that described oxygen-containing compound material is selected from least a in methyl alcohol, the dme; Described silicoaluminophosphamolecular molecular sieve is selected from least a among SAPO-5, SAPO-11, SAPO-17, SAPO-18, SAPO-34, SAPO-35, SAPO-44 or the SAPO-56; Described reactor is fast fluidized bed or riser tube.
3, be the method for low-carbon alkene according to the described oxygenate of claim 2, it is characterized in that described oxygen-containing compound material is selected from methyl alcohol; Described silicoaluminophosphamolecular molecular sieve is selected from SAPO-34; Described reactor is a fast fluidized bed.
4, be the method for low-carbon alkene according to the described oxygenate of claim 1, it is characterized in that the stripping medium in the described stripping zone is a water vapour; Lifting medium in the described catalyst transport standpipe is at least a in oxygenatedchemicals, water vapour or the reactor product that comprises methyl alcohol, dme; Described first part catalyzer is through returning the reaction zone bottom after the heat exchange, heat transferring medium is selected from water vapor.
5, be the method for low-carbon alkene according to the described oxygenate of claim 4, it is characterized in that the lifting medium in the described catalyst transport standpipe is the above hydrocarbon of oxygenatedchemicals, water vapour or C4 that comprises methyl alcohol, dme.
6, be the method for low-carbon alkene according to the described oxygenate of claim 5, it is characterized in that the lifting medium in the described catalyst transport standpipe is the above hydrocarbon of C4.
7, be the method for low-carbon alkene according to the described oxygenate of claim 1, it is characterized in that described condition for validity is: reaction pressure is counted 0～1MPa with gauge pressure, and temperature of reaction is 300～600 ℃, and the raw material weight hourly space velocity is 1～50 hour
-1, the average coke content of reaction zone catalyzer is 0.01～7% weight.
8, be the method for low-carbon alkene according to the described oxygenate of claim 7, it is characterized in that described condition for validity is: reaction pressure is counted 0.01～0.3MPa with gauge pressure, and temperature of reaction is 400～500 ℃, and the raw material weight hourly space velocity is 6～25 hours
-1, the average coke content of reaction zone catalyzer is 1～4% weight.
9, be the method for low-carbon alkene according to the described oxygenate of claim 1, it is characterized in that reclaimable catalyst that described second section enters revivifier by the catalyst transport pipeline accounts for 5～90% weight of total reclaimable catalyst; 10～100% weight of described regenerated catalyst enter in the catalyst transport standpipe, contact with the lifting medium.
10, be the method for low-carbon alkene according to the described oxygenate of claim 9, it is characterized in that reclaimable catalyst that described second section enters revivifier by the catalyst transport pipeline accounts for 15～40% weight of total reclaimable catalyst; 50～100% weight of described regenerated catalyst enter in the catalyst transport standpipe, contact with the lifting medium.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008101083561A CN101293803B (en) | 2008-04-11 | 2008-06-05 | Method for converting oxygen-containing compounds into low carbon olefin hydrocarbon |
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810043244.2 | 2008-04-11 | ||
| CN200810043244 | 2008-04-11 | ||
| CN200810043242 | 2008-04-11 | ||
| CN200810043242.3 | 2008-04-11 | ||
| CN2008101083561A CN101293803B (en) | 2008-04-11 | 2008-06-05 | Method for converting oxygen-containing compounds into low carbon olefin hydrocarbon |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101293803A true CN101293803A (en) | 2008-10-29 |
| CN101293803B CN101293803B (en) | 2011-08-17 |
Family
ID=40064384
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008101083561A Active CN101293803B (en) | 2008-04-11 | 2008-06-05 | Method for converting oxygen-containing compounds into low carbon olefin hydrocarbon |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101293803B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102276381A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Method for improving selectivity of light olefins prepared from conversion of oxygenated compound |
| CN102295507A (en) * | 2010-06-24 | 2011-12-28 | 中国石油化工股份有限公司 | Method for converting methanol or dimethyl ether into low-carbon olefin |
| CN103121901A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for converting oxygenated chemicals to generate low-carbon olefins |
| CN103121889A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Warm-taking method for preparing low-carbon olefin through conversion of oxygenated chemicals |
| CN103121890A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for producing low carbon olefin with oxygen compound |
| CN110437023A (en) * | 2019-07-12 | 2019-11-12 | 中国神华煤制油化工有限公司 | Prepare the method and alkene production system of alkene |
| CN113387763A (en) * | 2020-03-13 | 2021-09-14 | 中国石油化工股份有限公司 | Method for producing low-carbon olefin by using oxygen-containing compound |
| WO2021180150A1 (en) * | 2020-03-13 | 2021-09-16 | 中国石油化工股份有限公司 | Method for producing light olefin from oxygen-containing compound |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7053260B2 (en) * | 2002-01-07 | 2006-05-30 | Exxonmobil Chemical Patents Inc. | Reducing temperature differences within the regenerator of an oxygenate to olefin process |
-
2008
- 2008-06-05 CN CN2008101083561A patent/CN101293803B/en active Active
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102276381B (en) * | 2010-06-11 | 2014-04-23 | 中国石油化工股份有限公司 | Method for improving selectivity of light olefins prepared from conversion of oxygenated compound |
| CN102276381A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Method for improving selectivity of light olefins prepared from conversion of oxygenated compound |
| CN102295507B (en) * | 2010-06-24 | 2014-01-22 | 中国石油化工股份有限公司 | Method for converting methanol or dimethyl ether into low-carbon olefin |
| CN102295507A (en) * | 2010-06-24 | 2011-12-28 | 中国石油化工股份有限公司 | Method for converting methanol or dimethyl ether into low-carbon olefin |
| CN103121889A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Warm-taking method for preparing low-carbon olefin through conversion of oxygenated chemicals |
| CN103121890A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for producing low carbon olefin with oxygen compound |
| CN103121901A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for converting oxygenated chemicals to generate low-carbon olefins |
| CN103121890B (en) * | 2011-11-18 | 2015-01-07 | 中国石油化工股份有限公司 | Method for producing low carbon olefin with oxygen compound |
| CN103121901B (en) * | 2011-11-18 | 2015-09-09 | 中国石油化工股份有限公司 | The method of converting oxygen-containing compound to low-carbon olefins |
| CN110437023A (en) * | 2019-07-12 | 2019-11-12 | 中国神华煤制油化工有限公司 | Prepare the method and alkene production system of alkene |
| CN113387763A (en) * | 2020-03-13 | 2021-09-14 | 中国石油化工股份有限公司 | Method for producing low-carbon olefin by using oxygen-containing compound |
| WO2021180150A1 (en) * | 2020-03-13 | 2021-09-16 | 中国石油化工股份有限公司 | Method for producing light olefin from oxygen-containing compound |
| CN113387763B (en) * | 2020-03-13 | 2023-04-07 | 中国石油化工股份有限公司 | Method for producing low-carbon olefin by using oxygen-containing compound |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101293803B (en) | 2011-08-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101260013B (en) | Method for preparing low-carbon olefins from oxygen-containing compound | |
| CN101333141B (en) | Reaction device for conversing methanol or dimethyl ether to be low carbon olefin | |
| CN101270023B (en) | Method for improving yield of light olefin hydrocarbon | |
| CN101293803B (en) | Method for converting oxygen-containing compounds into low carbon olefin hydrocarbon | |
| CN101402538A (en) | Method for improving yield of light olefins | |
| CN101279877A (en) | Method for increasing yield of ethylene and propone in conversion process of oxocompound | |
| CN101270017B (en) | Process for producing light olefin hydrocarbon with oxygen-containing compound conversion | |
| CN102190550A (en) | Production method of low-carbon olefin | |
| CN101265150A (en) | Method for producing low-carbon olefins from oxygen-containing compound | |
| CN101239874A (en) | Reaction device for converting oxygen-containing compound to low-carbon olefins | |
| CN101260014B (en) | Method for producing low-carbon olefins from oxygen-containing compound | |
| CN101402539B (en) | Process for producing light olefins with methanol or dimethyl ether | |
| CN101318870B (en) | Process for improving yield of ethylene and propylene | |
| CN103739420A (en) | Method of increasing the yield of low-carbon olefins | |
| CN102464523B (en) | Method for producing light olefins | |
| CN102464524B (en) | Method for producing low-carbon olefins from methanol | |
| CN102295507B (en) | Method for converting methanol or dimethyl ether into low-carbon olefin | |
| CN101260015B (en) | Method for preparing low-carbon olefins from oxygen-containing compound | |
| CN102464535B (en) | Method for producing low carbon olefin from methanol or dimethyl ether | |
| CN102371137A (en) | Reaction device for converting methanol or dimethyl ether into light olefins | |
| CN102372542A (en) | Method for improving yield of ethylene and propylene | |
| CN102463074B (en) | Reaction device for producing low-carbon olefin from methanol or dimethyl ether | |
| CN102464528B (en) | Method for increasing yields of ethylene and propylene | |
| CN103772089A (en) | Reaction device for improving yield of ethylene and propylene | |
| CN103772088B (en) | Improve the method for ethene, propene yield |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |