CN107540503A - The method of oxygen-containing compound material ethene, propylene and aromatic hydrocarbons - Google Patents
The method of oxygen-containing compound material ethene, propylene and aromatic hydrocarbons 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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Abstract
The present invention relates to a kind of method of oxygen-containing compound material ethene, propylene and aromatic hydrocarbons, mainly solves the problems, such as that ethene, propene yield are low when ethene, propylene and aromatic hydrocarbons coproduction in the prior art.The present invention enters the product of aromatization reactor and the generation of regenerated catalyst haptoreaction rich in aromatic hydrocarbons by oxygen-containing compound material I from aromatization reactor bottom；Oxygen-containing compound material II enters the product of olefin hydrocarbon reactor and the generation of half reclaimable catalyst haptoreaction rich in ethene, propylene from olefin hydrocarbon reactor bottom；The carbon content of half reclaimable catalyst is 0.5~3% technical scheme, preferably solves the problem, available in ethene, propylene, arene industrial production.
Description
Technical field
The present invention relates to a kind of method of oxygen-containing compound material ethene, propylene and aromatic hydrocarbons.
Background technology
Ethene, propylene and aromatic hydrocarbons (especially triphen, benzene Benzene, toluene Toluene, dimethylbenzene Xylene, i.e. BTX)
It is important basic organic synthesis raw material.Driven by downstream derivative thing demand, the market demand of ethene, propylene and aromatic hydrocarbons continues
Increase.
It is ethene, propylene and virtue with the steam cracking process that liquid hydrocarbon (such as naphtha, diesel oil, secondary operation oil) is raw material
The main production of hydrocarbon.The technique belongs to petroleum path production technology, in recent years, due to the limited supply of petroleum resources and
Higher price, cost of material are continuously increased.By factor, alternative materials prepare ethene, propylene and aromatic hydrocarbons technology cause it is more next
More widely pay close attention to.Wherein, for coal-based methanol, dimethyl ether raw material, due to rich coal resources in China, it is increasingly becoming one kind
Important Chemical Manufacture raw material, turn into the important supplement of petroleum.Accordingly, it is considered to using methanol and/or dimethyl ether as raw material system
Standby ethene, propylene and aromatic hydrocarbons.
In various existing methanol, dimethyl ether catalysis transformation technology, the product of methanol/dimethyl ether conversion aromatic hydrocarbons is simultaneously
Including ethene, propylene and aromatic hydrocarbons.The technology initially sees Chang of Mobil companies in 1977 et al. (Journal of
Catalysis, 1977,47,249) report methanol and its oxygenatedchemicals conversion preparation virtue on ZSM-5 molecular sieve catalyst
The method of the hydrocarbons such as hydrocarbon.1985, Mobil companies disclosed first in its United States Patent (USP) applied US1590321
The result of study of methanol, dimethyl ether conversion aromatic hydrocarbons, it is catalyst that the research, which uses the phosphorous ZSM-5 molecular sieve for 2.7%, instead
It is 400~450 DEG C to answer temperature, methanol, dimethyl ether air speed 1.3 hours -1.
The relevant report and patent in the field are more, but the purpose product of most of technologies is aromatic hydrocarbons, ethene, propylene category
It is low in accessory substance, yield.Such as the patent in terms of methanol arenes catalytic agent：Chinese patent CN102372535,
CN102371176、CN102371177、CN102372550、CN102372536、CN102371178、CN102416342、
CN101550051, United States Patent (USP) US4615995, US2002/0099249A1 etc..Such as in terms of methanol aromatics process
Patent：United States Patent (USP) US4686312, Chinese patent ZL101244969, ZL1880288, CN101602646,
CN101823929, CN101671226, CN102199069, CN102199446, CN1880288 etc..
In addition, while technology path disclosed in some patents is methanol aromatic hydrocarbons co-producing light olefins, gasoline etc. other
Product, such as patent CN102775261, CN102146010, CN102531821, CN102190546, CN102372537.
Wherein, Multi-function methanol processing method disclosed in patent CN102775261 and device utilize methanol production low-carbon alkene
Hydrocarbon, gasoline, aromatic hydrocarbons.This method uses two-step method production technology, and first step methanol feedstock produces low under the effect of special-purpose catalyst 1
Carbon olefin, second step by the reaction gas containing low-carbon alkene after heat exchange, chilling, carrying out washing treatment, in the presence of special-purpose catalyst 2
Synthesize aromatic hydrocarbons and/or gasoline.The reactor of two courses of reaction can be fixed bed or fluid bed.This method uses two kinds of catalyst,
Technological process is complicated.
Patent CN102146010 discloses the work that low-carbon alkene and arene parallel cogeneration gasoline are produced using methanol as raw material
Skill.Low-carbon alkene and aromatic hydrocarbons are produced using methanol as raw material and using molecular sieve catalyst through methanol alkylation reaction and aromatization
Co-production gasoline.The reactor of methanol alkylation reaction and aromatization is various types of fixed bed reactors.
Patent CN102531821 discloses methanol and the method for the co-feeding production low-carbon alkene of naphtha and/or aromatic hydrocarbons,
Using load 2.2~6.0%La and 1.0~2.8%P ZSM-5 catalyst, fixed bed reactors or fluidized-bed reaction can be used
Device.Reaction temperature is 550~670 DEG C, air speed 1.0~5 hours -1.Methanol and naphtha are co-feeding in this method, using one
Reactor.
The method that patent CN102372537 and CN102190546 disclose preparing propylene by methanol transformation and aromatic hydrocarbons.This two specially
Profit is developed on the basis of preparing propylene by methanol transformation technology, and propylene is main purpose product, and aromatics yield is relatively low.
Technological process complexity, ethene, the problem of propylene and aromatics yield are low in above-mentioned patented technology all be present.Pin of the present invention
Technical scheme is proposed to property, solves above mentioned problem.
The content of the invention
Ethene, propylene are received when the technical problems to be solved by the invention are ethene, propylene and aromatic hydrocarbons coproduction in the prior art
The low technical problem of rate, there is provided a kind of method of oxygen-containing compound material ethene, propylene and aromatic hydrocarbons.This method have ethene,
The advantages of propene yield is high.
In order to solve the above technical problems, the technical solution adopted by the present invention is as follows：A kind of oxygen-containing compound material ethene,
The method of propylene and aromatic hydrocarbons, oxygen-containing compound material I (10) enter aromatization reactor (1) from aromatization reactor (1) bottom
With regenerated catalyst haptoreaction obtain rich in aromatic hydrocarbons product (11) and half reclaimable catalyst, half reclaimable catalyst it is to be generated through half
Inclined tube (4) enters olefin hydrocarbon reactor (2)；Oxygen-containing compound material II (12) enters olefine reaction from olefin hydrocarbon reactor (2) bottom
Device (2) and the generation of half reclaimable catalyst haptoreaction are rich in ethene, the product (13) and reclaimable catalyst of propylene；Reclaimable catalyst
Enter regenerator (3) regeneration through inclined tube to be generated (5) and obtain regenerated catalyst；Regenerated catalyst enters aromatization through regenerator sloped tube (6)
Change reactor (1)；Wherein, the carbon on half reclaimable catalyst, in terms of the mass percent of catalyst, content is 0.5~3%.
In above-mentioned technical proposal, the carbon on half reclaimable catalyst, in terms of the mass percent of catalyst, content be 0.8~
1.8%, preferably 0.8~1.3%.
In above-mentioned technical proposal, the temperature of aromatization reactor 1 is 440~520 DEG C, preferably 450~510 DEG C；Reactor
Internal catalyst bed layer density is 150~450 kilograms per cubic meter, preferably 200~400 kilograms per cubic meter；Oxygen-containing compound material I
10 mass space velocity is 0.1~5 hour-1, preferably 0.5~4 hour-1；Reaction pressure is calculated as 0~0.4 MPa, preferably 0 with gauge pressure
~0.3 MPa.
In above-mentioned technical proposal, the temperature of olefin hydrocarbon reactor (2) is 480~530 DEG C, preferably 490~520 DEG C；Reactor
Internal catalyst bed layer density is 80~450 kilograms per cubic meter, preferably 100~300 kilograms per cubic meter；Oxygen-containing compound material II
(12) mass space velocity is 0.5~6 hour-1, preferably 1~5 hour-1；Reaction pressure is calculated as 0~0.4 MPa, preferably 0 with gauge pressure
~0.3 MPa.
In above-mentioned technical proposal, the temperature of regenerator (3) is 550~720 DEG C, preferably 580~680 DEG C, more preferably 600~
650℃；0~0.4 MPa in terms of gauge pressure, preferably 0~0.3 MPa of regeneration pressure.
In above-mentioned technical proposal, the carbon in regenerated catalyst, in terms of the mass percent of catalyst, content is less than 0.1%.
In above-mentioned technical proposal, oxygen-containing compound material I (10) and oxygen-containing compound material II (12) include at least one
Select methanol, ethanol, normal propyl alcohol, isopropanol, C4~C20Alcohol, ethyl methyl ether, dimethyl ether, diethyl ether, Di Iso Propyl Ether, formaldehyde, carbon
Dimethyl phthalate, acetone, the compound of acetic acid, preferably methanol, ethanol, dimethyl ether, preferably methanol, dimethyl ether, ethanol.
In above-mentioned technical proposal, oxygenatedchemicals in oxygen-containing compound material I (10) and oxygen-containing compound material II (12)
Composition and/or content are identical or different, and the weight/mass percentage composition of oxygenatedchemicals is at least 10%, preferably at least 30%.
In above-mentioned technical proposal, the charge-mass ratio of oxygen-containing compound material I (10) and oxygen-containing compound material II (12)
For (9:1)~(4:6), preferably (8:2)~(5:5).
In above-mentioned technical proposal, catalyst activity component ZSM-5, ZSM-23, ZSM-11, beta-molecular sieve, Y molecular sieve or
The composite molecular screen formed each other, preferably ZSM-5；Carrier is kaolin, aluminum oxide, silica；Active component and carrier
Mass ratio be 10~50: 50~90, preferably 20~40: 60~80.
In above-mentioned technical proposal, catalyst is loaded with one or more elements or oxidation in Zn, Ag, P, Ga, Cu, Mn, Mg
Thing, preferably Zn, P；In terms of the mass percent of catalyst, the content of the element of load on a catalyst is 0.01~15%, excellent
Select 0.02~8%.
In above-mentioned technical proposal, the active component of catalyst is selected from ZSM-5 molecular sieve, with the percentage by weight of catalyst
Count, the Zn elements or oxide of load 0.01~5%, 0.1~8% P element or oxide on catalyst.
Oxygenatedchemicals aromatization process, oxygenatedchemicals are first dehydrated generation lower carbon number hydrocarbons, and lower carbon number hydrocarbons continues that aromatisation occurs
Reaction.Result of study shows that the catalyst activity and reaction condition that two-step reaction needs differ.It is active using low catalyst,
Short residence time can effectively suppress second step reaction, lower carbon number hydrocarbons is retained, while improve the selectivity of ethene, propylene.
Result of study shows that oxygenatedchemicals is 440~520 DEG C in temperature, and catalyst in reactor bed density is 150
~450 kilograms per cubic meter, mass space velocity is 0.1~5 hour-1, reaction pressure is calculated as sending out under conditions of 0~0.4 MPa with gauge pressure
Raw aromatization, obtains the product rich in aromatic hydrocarbons and coked catalyst that carbon content is 0.5~3%.It is catalyzed using the coking
Agent, it is 480~530 DEG C in temperature, catalyst in reactor bed density is 80~450 kilograms per cubic meter, and mass space velocity is
0.5~6 hour -1, under conditions of reaction pressure is calculated as 0~0.4 MPa with gauge pressure, oxygenatedchemicals continues reaction and can obtain richness
Product containing ethene, propylene.Therefore, two courses of reaction are combined, oxygenatedchemicals aromatization utilizes low carbon content, height
The regenerated catalyst of activity, the coked catalyst that the process obtains, i.e. half reclaimable catalyst, its activity can meet oxygen-containing chemical combination
Thing converts the requirement of ethene, propylene processed, thus realizes oxygenatedchemicals while prepares ethene, propylene and aromatic hydrocarbons.
In addition, this method can be according to market to ethene, propylene and aromatic hydrocarbons demand situation of change, it is clever within the specific limits
The inlet amount of two courses of reaction of modulation living, changes ethene, propylene, the yield of aromatic hydrocarbons.
Using technical scheme, raw material I and raw material II are methanol, and the mass ratio of raw material I and raw material II is 5:
5；The reaction temperature of aromatization reactor 1 is 490 DEG C, and catalyst in reactor bed density is 350 kilograms per cubic meter, methanol
Mass space velocity be 1.5 hours-1, reaction pressure is calculated as 0.25 MPa with gauge pressure；The reaction temperature of olefin hydrocarbon reactor 2 is 520 DEG C,
Catalyst in reactor bed density is 200 kilograms per cubic meter, and the mass space velocity of methanol is 3 hours-1, reaction pressure is with gauge pressure
It is calculated as 0.25 MPa；Carbon on half reclaimable catalyst, in terms of the mass percent of catalyst, content 1.3%；Regenerator 3
Temperature be 650 DEG C, 0.25 MPa in terms of gauge pressure of regeneration pressure；Using modified ZSM-5 catalyst；Ethene carbon base absorption rate is
16.1%th, propylene carbon base absorption rate be 12.0%, aromatic hydrocarbons carbon base absorption rate be 51.8%.
Brief description of the drawings
Fig. 1 is the reaction unit schematic diagram of the present invention.
In Fig. 1,1 is aromatization reactor；2 be olefin hydrocarbon reactor；3 be regenerator；4 be half inclined tube to be generated；5 be to be generated oblique
Pipe；6 be regenerator sloped tube；7 be aromatization reactor cyclone separator；8 be olefin hydrocarbon reactor cyclone separator；9 be that regenerator revolves
Wind separator；10 be to contain oxygen-containing compound material I；11 be aromatization reactor reaction product；12 be to contain oxygenatedchemicals
Raw material II；13 be olefin hydrocarbon reactor reaction product；14 be main wind；15 be flue gas；16 be overall reaction product.
Oxygen-containing compound material I 10 enters aromatization reactor 1 in Fig. 1, and regenerated catalyst haptoreaction, generation are rich in
The reclaimable catalyst of aromatization reactor reaction product 11 and half of aromatic hydrocarbons；Half reclaimable catalyst enters alkene through half inclined tube 4 to be generated
Reactor 2；Oxygen-containing compound material II 12 enters olefin hydrocarbon reactor 1, and half reclaimable catalyst haptoreaction, and generation is rich in alkene
Olefin hydrocarbon reactor reaction product 13 and reclaimable catalyst；Aromatization reactor reaction product 11 and olefin hydrocarbon reactor reaction product
13 converge to form overall reaction product 16 and enter subsequent separation system；Reclaimable catalyst enters regenerator 3 through inclined tube 5 to be generated, and main
The contact burn-up carbon of wind 14, obtains regenerated catalyst and flue gas 15；Regenerated catalyst enters aromatization reactor 1 through regenerator sloped tube 6.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Embodiment
【Embodiment 1】
Using circulating fluid bed reaction device as shown in Figure 1.Raw material 10 is methanol, and raw material 12 is ethanol, the He of raw material 10
The charge-mass ratio of raw material 12 is 8:2.The reaction temperature of aromatization reactor 1 is 440 DEG C, catalyst in reactor bed density
For 450 kilograms per cubic meter, the mass space velocity of methanol is 0.1 hour-1, reaction pressure is calculated as 0 MPa with gauge pressure；Olefin hydrocarbon reactor 2
Reaction temperature be 480 DEG C, catalyst in reactor bed density is 450 kilograms per cubic meter, and the mass space velocity of methanol is 0.5
Hour-1, reaction pressure is calculated as 0 MPa with gauge pressure；The temperature of regenerator 3 is 550 DEG C, 0 MPa in terms of gauge pressure of regeneration pressure；Partly treat
Carbon on raw catalyst, in terms of the mass percent of catalyst, content 3%.Using Ag-ZSM-5 catalyst, Ag constituent contents
For 1.3%, the mass ratio of ZSM-5 molecular sieve and matrix is 4:6, the silicoaluminophosphate molecular ratio of ZSM-5 molecular sieve is 25.Reaction result is shown in
Table 1.
【Embodiment 2】
Using circulating fluid bed reaction device as shown in Figure 1.Raw material 10 is methanol, and raw material 12 is dimethyl ether, raw material 10
Charge-mass ratio with raw material 12 is 6:4.The reaction temperature of aromatization reactor 1 is 520 DEG C, and catalyst in reactor bed is close
Spend for 150 kilograms per cubic meter, the mass space velocity of methanol is 5 hours-1, reaction pressure is calculated as 0.4 MPa with gauge pressure；Olefine reaction
The reaction temperature of device 2 is 530 DEG C, and catalyst in reactor bed density is 80 kilograms per cubic meter, and the mass space velocity of methanol is 6
Hour-1, reaction pressure is calculated as 0.4 MPa with gauge pressure；The temperature of regenerator 3 is 720 DEG C, 0.4 MPa in terms of gauge pressure of regeneration pressure；
Carbon on half reclaimable catalyst, in terms of the mass percent of catalyst, content 0.5%.Using Mn-ZSM-11 catalyst,
ZSM-11 molecular sieves and the mass ratio of matrix are 3:7；The silicoaluminophosphate molecular ratio of ZSM-11 molecular sieves is 50；Matrix is kaolin and three
The mixture of Al 2 O, both mass ratioes are 7:3, Mn constituent contents are 9.09%.Reaction result is shown in Table 1.
【Embodiment 3】
Using circulating fluid bed reaction device as shown in Figure 1.Raw material 10 and 12 is dimethyl ether, raw material 10 and raw material 12
Charge-mass ratio be 9:1.The reaction temperature of aromatization reactor 1 is 470 DEG C, and catalyst in reactor bed density is 400
Kilograms per cubic meter, the mass space velocity of methanol is 2 hours-1, reaction pressure is calculated as 0.25 MPa with gauge pressure；Olefin hydrocarbon reactor 2 it is anti-
It is 520 DEG C to answer temperature, and catalyst in reactor bed density is 200 kilograms per cubic meter, and the mass space velocity of methanol is 3 hours-1,
Reaction pressure is calculated as 0.25 MPa with gauge pressure；The temperature of regenerator 3 is 650 DEG C, 0.25 MPa in terms of gauge pressure of regeneration pressure；Partly treat
Carbon on raw catalyst, in terms of the mass percent of catalyst, content 1.3%.Using ZSM-5- beta catalysts, ZSM-5 and β
Molecular sieve and the mass ratio of matrix are 3.5: 6.5.The silicoaluminophosphate molecular ratio of ZSM-5 molecular sieve is 38；The silicoaluminophosphate molecular ratio of beta-molecular sieve
For 20；The mass ratio of ZSM-5 and beta-molecular sieve is 9:1.Reaction result is shown in Table 1.
【Embodiment 4】
Using circulating fluid bed reaction device as shown in Figure 1.Raw material 10 and 12 is methanol, raw material 10 and raw material 12
Charge-mass ratio is 7:3.The reaction temperature of aromatization reactor 1 is 470 DEG C, and catalyst in reactor bed density is 400,000
Gram/cubic metre, the mass space velocity of methanol is 1 hour-1, reaction pressure is calculated as 0.15 MPa with gauge pressure；The reaction of olefin hydrocarbon reactor 2
Temperature is 500 DEG C, and catalyst in reactor bed density is 300 kilograms per cubic meter, and the mass space velocity of methanol is 2.5 hours-1,
Reaction pressure is calculated as 0.15 MPa with gauge pressure；The temperature of regenerator 3 is 600 DEG C, 0.15 MPa in terms of gauge pressure of regeneration pressure；Partly treat
Carbon on raw catalyst, in terms of the mass percent of catalyst, content 0.8%.Using Zn-P-ZSM-5 catalyst, ZSM-5
Molecular sieve and the mass ratio of matrix are 3.5:6.5；The silicoaluminophosphate molecular ratio of ZSM-5 molecular sieve is 25；Matrix is kaolin and three oxygen
Change the mixture of two aluminium, both mass ratioes are 7:3, Zn constituent contents are 2.87%, and P element content is 1.48%.Reaction knot
Fruit is shown in Table 1.
【Embodiment 5】
Using the reaction unit and catalyst of embodiment 4, the species and flow of raw material 10 and 12 are and the holding of embodiment 3 one
Cause.The reaction temperature of aromatization reactor 1 is 480 DEG C, and catalyst in reactor bed density is 350 kilograms per cubic meter, methanol
Mass space velocity be 1.5 hours-1, reaction pressure is calculated as 0.25 MPa with gauge pressure；The reaction temperature of olefin hydrocarbon reactor 2 is 520 DEG C,
Catalyst in reactor bed density is 350 kilograms per cubic meter, and the mass space velocity of methanol is 3 hours-1, reaction pressure is with gauge pressure
It is calculated as 0.25 MPa；The temperature of regenerator 3 is 650 DEG C, 0.25 MPa in terms of gauge pressure of regeneration pressure；On half reclaimable catalyst
Carbon, in terms of the mass percent of catalyst, content 1.3%.Reaction result is shown in Table 1.
【Embodiment 6】
Using the reaction unit and catalyst of embodiment 4, the species and flow of raw material 10 and 12 are and the holding of embodiment 3 one
Cause.The reaction temperature of aromatization reactor 1 is 500 DEG C, and catalyst in reactor bed density is 300 kilograms per cubic meter, methanol
Mass space velocity be 1.5 hours-1, reaction pressure is calculated as 0.2 MPa with gauge pressure；The reaction temperature of olefin hydrocarbon reactor 2 is 530 DEG C,
Catalyst in reactor bed density is 200 kilograms per cubic meter, and the mass space velocity of methanol is 3 hours-1, reaction pressure is with gauge pressure
It is calculated as 0.2 MPa；The temperature of regenerator 3 is 650 DEG C, 0.25 MPa in terms of gauge pressure of regeneration pressure；Carbon on half reclaimable catalyst,
In terms of the mass percent of catalyst, content 1.8%.Reaction result is shown in Table 1.
【Comparative example 1】
Using the reaction unit and catalyst of embodiment 4, the species and flow of raw material 10 and 12 are and the holding of embodiment 3 one
Cause.The reaction temperature of aromatization reactor 1 is 530 DEG C, and catalyst in reactor bed density is 140 kilograms per cubic meter, methanol
Mass space velocity be 6 hours-1, reaction pressure is calculated as 0.5 MPa with gauge pressure；The reaction temperature of olefin hydrocarbon reactor 2 is 540 DEG C, instead
It is 70 kilograms per cubic meter to answer device internal catalyst bed layer density, and the mass space velocity of methanol is 7 hours-1, reaction pressure is calculated as with gauge pressure
0.5 MPa；The temperature of regenerator 3 is 680 DEG C, 0.5 MPa in terms of gauge pressure of regeneration pressure；Carbon on half reclaimable catalyst, to urge
The mass percent meter of agent, content 3.2%.Reaction result is shown in Table 1.
【Comparative example 2】
Using the reaction unit and catalyst of embodiment 4, the species and flow of raw material 10 and 12 are and the holding of embodiment 3 one
Cause.The reaction temperature of aromatization reactor 1 is 430 DEG C, and catalyst in reactor bed density is 460 kilograms per cubic meter, methanol
Mass space velocity be 0.07 hour-1, reaction pressure is calculated as 0.02 MPa with gauge pressure；The reaction temperature of olefin hydrocarbon reactor 2 is 470
DEG C, catalyst in reactor bed density is 460 kilograms per cubic meter, and the mass space velocity of methanol is 0.4 hour-1, reaction pressure with
Gauge pressure is calculated as 0.02 MPa；The temperature of regenerator 3 is 680 DEG C, 0.05 MPa in terms of gauge pressure of regeneration pressure；On half reclaimable catalyst
Carbon, in terms of the mass percent of catalyst, content 0.4%.Reaction result is shown in Table 1.
Table 1
| One way ethene carbon base absorption rate, % | Once-through propylene carbon base absorption rate, % | One way aromatic hydrocarbons carbon base absorption rate, % | |
| Embodiment 1 | 14.8 | 10.4 | 50.4 |
| Embodiment 2 | 13.8 | 6.5 | 56.3 |
| Embodiment 3 | 16.1 | 12 | 51.8 |
| Embodiment 4 | 16.7 | 10.3 | 50.2 |
| Embodiment 5 | 18.3 | 14.1 | 43.7 |
| Embodiment 6 | 13.4 | 9.8 | 54.1 |
| Comparative example 1 | 17.4 | 13.7 | 39.7 |
| Comparative example 2 | 12.4 | 8.7 | 50.7 |
Claims (10)
1. a kind of method of oxygen-containing compound material ethene, propylene and aromatic hydrocarbons, oxygen-containing compound material I (10) are anti-from aromatisation
Answer the product (11) and half that device (1) bottom enters aromatization reactor (1) and regenerated catalyst haptoreaction obtains being rich in aromatic hydrocarbons
Reclaimable catalyst, half reclaimable catalyst enter olefin hydrocarbon reactor (2) through half inclined tube (4) to be generated；Oxygen-containing compound material II (12)
Enter olefin hydrocarbon reactor (2) from olefin hydrocarbon reactor (2) bottom and the generation of half reclaimable catalyst haptoreaction is rich in ethene, propylene
Product (13) and reclaimable catalyst；Reclaimable catalyst enters regenerator (3) regeneration through inclined tube to be generated (5) and obtains regenerated catalyst；
Regenerated catalyst enters aromatization reactor (1) through regenerator sloped tube (6)；Wherein, the carbon on half reclaimable catalyst, with catalyst
Mass percent meter, content are 0.5~3%.
2. the method for oxygen-containing compound material ethene according to claim 1, propylene and aromatic hydrocarbons, it is characterised in that partly treat
Carbon on raw catalyst, in terms of the mass percent of catalyst, content is 0.8~1.8%.
3. the method for oxygen-containing compound material ethene according to claim 2, propylene and aromatic hydrocarbons, it is characterised in that partly treat
Carbon on raw catalyst, in terms of the mass percent of catalyst, content is 0.8~1.3%.
4. the method for oxygen-containing compound material ethene according to claim 1, propylene and aromatic hydrocarbons, it is characterised in that aromatization
The temperature for changing reactor (1) is 440~520 DEG C, and catalyst in reactor bed density is 150~450 kilograms per cubic meter, is contained
The mass space velocity of oxygenate feedstock I (10) is 0.1~5 hour-1, reaction pressure is calculated as 0~0.4 MPa with gauge pressure.
5. the method for oxygen-containing compound material ethene according to claim 1, propylene and aromatic hydrocarbons, it is characterised in that alkene
The temperature of reactor (2) is 480~530 DEG C, and catalyst in reactor bed density is 80~450 kilograms per cubic meter, containing oxidation
The mass space velocity of compound raw material II (12) is 0.5~6 hour-1, reaction pressure is calculated as 0~0.4 MPa with gauge pressure.
6. the method for oxygen-containing compound material ethene according to claim 1, propylene and aromatic hydrocarbons, it is characterised in that regeneration
The temperature of device (3) is 550~720 DEG C, 0~0.4 MPa in terms of gauge pressure of regeneration pressure.
7. the method for oxygen-containing compound material ethene according to claim 1, propylene and aromatic hydrocarbons, it is characterised in that regeneration
Carbon on catalyst, in terms of the mass percent of catalyst, content is less than 0.1%.
8. the method for oxygen-containing compound material ethene according to claim 1, propylene and aromatic hydrocarbons, it is characterised in that oxygen-containing
Raw materials of compound I (10) and oxygen-containing compound material II (12) are included selected from methanol, ethanol, normal propyl alcohol, isopropanol, C4~C20
At least one of alcohol, ethyl methyl ether, dimethyl ether, diethyl ether, Di Iso Propyl Ether, formaldehyde, dimethyl carbonate, acetone and acetic acid chemical combination
Thing, the weight/mass percentage composition of oxygenatedchemicals is at least 10%.
9. the method for oxygen-containing compound material ethene according to claim 8, propylene and aromatic hydrocarbons, it is characterised in that oxygen-containing
Oxygenatedchemicals composition and/or content are identical or different in raw materials of compound I (10) and oxygen-containing compound material II (12).
10. the method for oxygen-containing compound material ethene according to claim 8, propylene and aromatic hydrocarbons, it is characterised in that contain
The charge-mass ratio of oxygenate feedstock I (10) and oxygen-containing compound material II (12) is (9:1)~(4:6).
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| CN201610498408.5A CN107540503B (en) | 2016-06-29 | 2016-06-29 | Method for preparing ethylene, propylene and aromatic hydrocarbon from oxygen-containing compound raw material |
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| CN201610498408.5A CN107540503B (en) | 2016-06-29 | 2016-06-29 | Method for preparing ethylene, propylene and aromatic hydrocarbon from oxygen-containing compound raw material |
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| CN111100664A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Method for preparing aromatic hydrocarbon by catalytic conversion of methanol |
| WO2022057807A1 (en) * | 2020-09-15 | 2022-03-24 | 中国石油化工股份有限公司 | Method for preparing ethylene propylene |
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| EP3040324A1 (en) * | 2014-12-30 | 2016-07-06 | Shell Internationale Research Maatschappij B.V. | A Process for Converting Oxygenates to Olefins and Aromatics |
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| CN104557361A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Multifunctional system and method for preparing ethylene, propylene and aromatic hydrocarbons by converting methanol and/or dimethyl ether |
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| CN111100664A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Method for preparing aromatic hydrocarbon by catalytic conversion of methanol |
| CN111100664B (en) * | 2018-10-25 | 2021-06-18 | 中国石油化工股份有限公司 | Method for preparing aromatic hydrocarbon by catalytic conversion of methanol |
| WO2022057807A1 (en) * | 2020-09-15 | 2022-03-24 | 中国石油化工股份有限公司 | Method for preparing ethylene propylene |
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