CN107963957B - Method and device for preparing propylene and C4 hydrocarbon - Google Patents
Method and device for preparing propylene and C4 hydrocarbon Download PDFInfo
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- CN107963957B CN107963957B CN201610910680.XA CN201610910680A CN107963957B CN 107963957 B CN107963957 B CN 107963957B CN 201610910680 A CN201610910680 A CN 201610910680A CN 107963957 B CN107963957 B CN 107963957B
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- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
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- C—CHEMISTRY; METALLURGY
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- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/82—Phosphates
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- C07C2529/85—Silicoaluminophosphates (SAPO compounds)
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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 invention relates to a method for preparing propylene and C4 hydrocarbon from oxygen-containing compound and a device thereof. According to the method, more than 80 wt.% of hydrocarbons with the carbon number of more than 5 in the product are circulated to the catalytic cracking riser to carry out cracking reaction, so that the product containing propylene and C4 hydrocarbons is generated, the reaction rate of the ethylene alkylation reaction is improved, and the unit volume capacity of the reactor is high.
Description
Technical Field
The invention relates to the field of chemical catalysis, in particular to a method and a device for preparing propylene and C4 hydrocarbons from oxygen-containing compounds.
Background
Propylene and butadiene are important chemical raw materials, and are generally obtained from naphtha cracking and steam cracking. The main sources of propylene are ethylene co-production propylene and refinery by-product propylene, while the main source of butadiene is obtained by further processing the C4 by-product produced in the ethylene cracking process. In recent years, Methanol To Olefin (MTO) technology, Methanol To Propylene (MTP) technology, ethane dehydrogenation to ethylene technology, and propane dehydrogenation to propylene technology have been developed rapidly, and the global trend of light olefin feedstock is obvious, which leads to a shortage of C4 resource supply, so that it is necessary to develop a process capable of preparing propylene and C4 olefin with high selectivity, thereby meeting the market demand.
German Lurgi company develops a fixed bed methanol-to-olefin technology (WO2004/018089), which utilizes a ZSM-5 molecular sieve catalyst of southern chemical company to perform a methanol-to-olefin reaction in a fixed bed reactor, wherein the propylene selectivity is close to 70%, and byproducts are ethylene, liquefied petroleum gas and gasoline.
The DMTO technology developed by the large-scale continuous substance takes SAPO molecular sieve as a catalyst, a dense-phase circulating fluidized bed reactor is used, methanol aqueous solution is taken as a raw material, the yield of ethylene and propylene in the product is about 80 percent, and more than 10 percent of C4 hydrocarbon is byproduct.
Patent CN104098429A discloses a method for preparing propylene and C4 hydrocarbons from methanol by using a circulating fluidized bed, which uses a ZSM-5 catalyst, and is characterized in that the raw material methanol and most of C1, C2 and C5 hydrocarbons in the product are jointly fed into the circulating fluidized bed reactor, and propylene, C4 hydrocarbons, C6 hydrocarbons and by-products are recovered as final products.
Patent CN101177374B discloses a process for preparing olefins from methanol or dimethyl ether. The method comprises a methanol or dimethyl ether conversion reaction, an ethylene and methanol alkylation reaction and a catalytic cracking reaction of heavy components above C4. The conversion reaction of methanol or dimethyl ether and the alkylation reaction of ethylene and methanol adopt a catalyst 1 to complete the reaction in the same reactor; the catalytic cracking reaction of heavy components above C4 is completed in another reactor by using catalyst 2.
The processes disclosed in patents CN104098429A and CN101177374B have a common feature of increasing the selectivity of the target products (propylene and C4) by recycling light components (hydrocarbons with carbon number not more than 2). The main reaction of the light component recycle reaction is the alkylation reaction of ethylene and methanol.
Both the MTO reaction and the olefin alkylation reactions can use acidic molecular sieve catalysts, but the MTO reaction rate is much higher than the olefin alkylation reaction. Through researches, the fresh SAPO catalyst has high activity and is more beneficial to olefin alkylation reaction, and after the catalyst is deposited with carbon, the olefin alkylation reaction rate can be rapidly reduced.
Methanol is a feedstock for both the olefin alkylation reaction and the MTO reaction, and therefore, the olefin alkylation reaction is necessarily accompanied by the MTO reaction. The MTO reaction results in carbon build-up and reduced activity of the catalyst, which inhibits the olefin alkylation reaction. Increasing the olefin alkylation reaction rate reduces the light component content of the product gas and thus increases the capacity per unit volume of the reactor.
The methods disclosed in patents CN104098429A and CN101177374B do not relate to the reactor structure, nor do they specify the catalyst flow pattern, the raw material distribution pattern, etc. in the reactor. The method disclosed in patent CN101177374B uses SAPO catalyst, and the examples show that the mass ratio of methanol to light components is 1:10-20, so it can be seen that the content of light components is extremely high and the productivity per unit volume of the reactor is extremely low. The process disclosed in patent CN104098429A uses ZSM-5 catalyst, the content of hydrocarbons above C6 in the product is high, and the content of light components in the product gas is not disclosed in the process.
The preparation of propylene and C4 hydrocarbons by using methanol and/or dimethyl ether as raw materials necessarily generates a certain amount of hydrocarbons above C5 simultaneously. The hydrocarbons with the carbon number of more than 5 have low economic value, and the hydrocarbons with the carbon number of more than 5 can be converted into ethylene, propylene, C4 hydrocarbons and the like through catalytic cracking reaction, so that the selectivity of the propylene and the C4 hydrocarbons can be improved.
From the above analysis, the main reactions for preparing propylene and C4 hydrocarbons from methanol are MTO reaction and olefin alkylation reaction, and therefore, the key to improving the selectivity of propylene and C4 hydrocarbons is the catalyst design and reactor design. Avoiding suppression of the olefin alkylation reaction by MTO reaction through reactor optimization is one of the important methods to improve the economics of the methanol to propylene and C4 hydrocarbons process.
Disclosure of Invention
The invention provides a novel method and a device for improving the reaction rate of the vinyl alkylation, aiming at the problem of low reaction rate of the vinyl alkylation in the process of preparing propylene and C4 hydrocarbon from methanol. The method is used for producing propylene and C4 hydrocarbon by using oxygen-containing compounds, and has the advantages of high yield of propylene and C4 hydrocarbon and good economical efficiency of the process.
To achieve the above objects, in one aspect, the present invention provides an apparatus for producing propylene and C4 hydrocarbons from oxygenates, the apparatus comprising:
a) a turbulent fluidized bed reactor (1), wherein the rapid fluidized bed reactor (1) comprises a reactor shell (2), n reactor feeding distributors (3-1-3-n), reactor gas-solid separators 1(4), reactor gas-solid separators 2(5), a reactor heat collector (6), a product gas outlet (7) and a reactor stripper (8), wherein the lower part of the turbulent fluidized bed reactor (1) is a reaction zone, the upper part of the turbulent fluidized bed reactor (1) is a settling zone, the n reactor feeding distributors (3-1-3-n) are arranged in the reaction zone (preferably the n reactor feeding distributors are arranged in the reaction zone from bottom to top, 0< n <10), the reactor heat collector (6) is arranged in the reaction zone, the reactor gas-solid separators 1(4) and the reactor gas-solid separators 2(5) are arranged outside the settling zone or the reactor shell (2), the inlet of the reactor gas-solid separator 1(4) is connected with the regeneration riser 24, the catalyst outlet of the reactor gas-solid separator 1(4) is arranged at the bottom of the reaction zone, the gas outlet of the reactor gas-solid separator 1(4) is arranged in the settling zone, the inlet of the reactor gas-solid separator 2(5) is arranged in the settling zone, the catalyst outlet of the reactor gas-solid separator 2(5) is arranged in the reaction zone, the gas outlet of the reactor gas-solid separator 2(5) is connected with the product gas outlet (7), and the reactor stripper (8) passes through the reactor shell (2) from outside to inside at the bottom of the turbulent fluidized bed reactor (1) and is opened in the reaction zone of the turbulent fluidized bed reactor (1) (preferably, the opening of the reactor stripper inside the reactor shell has the horizontal height higher than the height of the reaction zone of 1/10);
b) a catalytic cracking riser (28), the bottom of the catalytic cracking riser (28) is connected with the outlet of the catalytic cracking inclined tube (26) and is provided with a hydrocarbon inlet (29) above C5, and the outlet of the catalytic cracking riser (28) is connected with the settling zone of the turbulent fluidized bed reactor (1);
c) a fluidized bed regenerator (14), the fluidized bed regenerator (14) comprising a regenerator housing (15), a regenerator feed distributor (16), a regenerator gas-solid separator (17), a regenerator heat extractor (18), a flue gas outlet (19) and a regenerator stripper (20), the lower part of the fluidized bed regenerator (14) is a regeneration zone, the upper part of the fluidized bed regenerator (14) is a settling zone, a regenerator feed distributor (16) is arranged at the bottom of the regeneration zone, a regenerator heat extractor (18) is arranged in the regeneration zone, a regenerator gas-solid separator (17) is arranged outside the settling zone or a regenerator shell (15), an inlet of the regenerator gas-solid separator (17) is arranged in the settling zone, a catalyst outlet of the regenerator gas-solid separator (17) is arranged in the regeneration zone, a gas outlet of the regenerator gas-solid separator (17) is connected with a flue gas outlet (19), and a regenerator stripper (20) is opened at the bottom of the regenerator shell (15);
d) the bottom of a reactor stripper (8) is provided with a reactor stripping gas inlet (9), the bottom of the reactor stripper (8) is connected with the inlet of a to-be-regenerated inclined pipe (10), a to-be-regenerated slide valve (11) is arranged in the to-be-regenerated inclined pipe (10), the outlet of the to-be-regenerated inclined pipe (10) is connected with the inlet of a to-be-regenerated lifting pipe (12), the bottom of the to-be-regenerated lifting pipe (12) is provided with a to-be-regenerated lifting gas inlet (13), and the outlet of the to-be-regenerated lifting pipe (12) is connected with the settling section of a fluidized bed regenerator (14);
e) the bottom of the regenerator stripper (20) is provided with a regenerator stripping gas inlet (21), the bottom of the regenerator stripper (20) is connected with the inlet of a regeneration inclined tube (22), a regeneration slide valve (23) is arranged in the regeneration inclined tube (22), the outlet of the regeneration inclined tube (22) is connected with the inlet of a regeneration lifting tube (24), the bottom of the regeneration lifting tube (24) is provided with a regeneration lifting gas inlet (25), and the outlet of the regeneration lifting tube (24) is connected with the inlet of a reactor gas-solid separator 1 (4);
the bottom of the regenerator stripper (20) is also connected to the inlet of a catalytic cracking inclined tube (26) in which a catalytic cracking slide valve (27) is arranged.
In another aspect, the present invention provides a process for producing propylene and C4 hydrocarbons from oxygenates, comprising:
a) introducing a raw material containing oxygen-containing compounds into a reaction zone of a turbulent fluidized bed reactor (1) from n reactor feeding distributors (3-1-3-n), and contacting the raw material with a catalyst to generate a material flow containing propylene and C4 hydrocarbon products and a carbon-containing spent catalyst;
b) the spent catalyst is regenerated by a fluidized bed regenerator (14) to form a regenerated catalyst, one part of the regenerated catalyst enters the bottom of a reaction zone in the turbulent fluidized bed reactor (1) after gas-solid separation of a gas-solid separator 1(4) of the reactor, and the other part of the regenerated catalyst enters a catalytic cracking riser (28) through a catalytic cracking inclined tube (26);
c) will be driven by turbulenceSending a stream containing propylene and C4 hydrocarbon products flowing out of the fluidized bed reactor (1) into a product separation system, and separating to obtain propylene, C4 hydrocarbons, light components, propane and hydrocarbons above C5, wherein the light components contain more than 90 wt% of ethylene and small amounts of methane, ethane, hydrogen, CO and CO2More than 70 wt.% of the light components are returned to the reaction zone of the turbulent fluidized bed reactor (1) from the lowermost reactor feed distributor (3-1) of the turbulent fluidized bed reactor (1), the alkylation of ethylene and oxygenate occurs over the catalyst to produce a product comprising propylene, and less than 30 wt.% of the light components are recovered as by-products;
d) more than 80 wt.% of the hydrocarbons with more than C5 from the separation system enter the catalytic cracking riser (28) from the hydrocarbon inlet (29) with more than C5 and are in concurrent contact with the regenerated catalyst from the catalytic cracking inclined tube (26) to carry out cracking reaction to generate a stream containing propylene and C4 hydrocarbons and carbon-containing catalyst, then the stream containing propylene and C4 hydrocarbons and the carbon-containing catalyst enter a settling zone of the turbulent fluidized bed reactor (1) through the outlet of the catalytic cracking riser (28), and less than 20 wt.% of the hydrocarbons with more than C5 are recovered as byproducts.
Preferably, the process of the present invention is carried out with an apparatus for the production of propylene and C4 hydrocarbons from oxygenates according to the first aspect, wherein
The spent catalyst enters a settling section of a fluidized bed regenerator (14) through a reactor stripper (8), a spent inclined tube (10), a spent slide valve (11) and a spent riser (12);
introducing a regeneration medium into a regeneration zone of a fluidized bed regenerator (14) from a regenerator feed distributor (16), and carrying out a carbon burning reaction on the regeneration medium and a spent catalyst to generate a catalyst containing CO and CO2The flue gas and the regenerated catalyst are discharged after being dedusted by a gas-solid separator (17) of the regenerator;
a part of regenerated catalyst enters an inlet of a gas-solid separator 1(4) of the reactor through a regenerator stripper (20), a regeneration inclined tube (22), a regeneration slide valve (23) and a regeneration lifting tube (24), and after gas-solid separation, the regenerated catalyst enters the bottom of a reaction zone in the turbulent fluidized bed reactor (1); the other part of the regenerated catalyst enters a catalytic cracking riser (28) through a regenerator stripper (20), a catalytic cracking inclined tube (26) and a catalytic cracking slide valve (27);
the reactor stripping gas enters a reactor stripper (8) from a reactor stripping gas inlet (9) to be in countercurrent contact with the spent catalyst, and then enters a turbulent fluidized bed reactor (1); spent lifting gas enters a spent lifting pipe (12) from a spent lifting gas inlet (13) to be in concurrent flow contact with a spent catalyst, and then enters a settling section of a fluidized bed regenerator (14);
the regenerator stripping gas enters a regenerator stripper (20) from a regenerator stripping gas inlet (21) to be in countercurrent contact with the regenerated catalyst and then enters a fluidized bed regenerator (14); the regenerated lift gas enters a regenerated lift pipe (24) from a regenerated lift gas inlet (25) to be contacted with the regenerated catalyst in a concurrent flow manner, and then enters an inlet of a gas-solid separator 1(4) of the reactor.
The turbulent fluidized bed reactor is mainly characterized in that light components enter from a reactor feeding distributor at the bottom, oxygen-containing compounds enter from n reactor feeding distributors respectively, and regenerated catalysts directly enter the bottom of a reaction zone. On one hand, the catalyst has high activity at the lower part of the reaction zone, which is beneficial to the alkylation reaction of ethylene, propylene and methanol; on the other hand, because the mode of multistage feeding of the oxygen-containing compound is adopted, the oxygen-containing compound is prevented from completing most of conversion reaction in a small part of area below the reaction area, so that the concentration of the oxygen-containing compound in most of the reaction area is uniform, and the inhibition of MTO reaction on the olefin alkylation reaction is weakened. Therefore, the turbulent fluidized bed reactor can effectively improve the reaction rate of the olefin alkylation, and the unit volume capacity of the reactor is high.
The catalytic cracking riser of the present invention is mainly characterized in that its outlet is directly connected to the settling zone of the turbulent fluidized bed reactor, and the turbulent fluidized bed reactor shares the gas-solid separator 2.
The fluidized bed regenerator in the present invention is preferably a turbulent fluidized bed regenerator.
The reactor gas-solid separator 1, the reactor gas-solid separator 2 and the regenerator gas-solid separator in the present invention are preferably cyclones.
In the method, products such as ethylene, propylene and the like are generated by MTO reaction, ethylene, propylene and the like are consumed by olefin alkylation reaction, the ethylene alkylation reaction rate is high, and the light component content and the light component circulation amount in product gas are low. In the process of the invention, the light component recycle is from 5 to 40 wt.% of the oxygenate feed.
In the method of the invention, the hydrocarbons with more than C5 circulate in the system, and the circulating amount of the hydrocarbons with more than C5 is 2-20 wt.% of the feeding amount of the oxygen-containing compounds.
According to the method, more than 70 wt% of light components and more than 80 wt% of hydrocarbons above C5 are circulated in the system, and the release rate of the light components and the hydrocarbons above C5 influences the composition of the product gas in an equilibrium state. At equilibrium, the composition of the product gas is 20-50 wt.% propylene, 15-40 wt.% C4 hydrocarbons, 10-45 wt.% light components, 0-5 wt.% propane, and 5-20 wt.% hydrocarbons above C5. The light fraction containing more than 90 wt%, for example>95 wt.% ethylene, the other components being methane, ethane, hydrogen, CO and CO2And the like.
In a preferred embodiment, the catalyst contains a SAPO molecular sieve, which has the functions of both methanol to olefins, olefin alkylation and catalytic cracking.
In a preferred embodiment, the regenerated catalyst carbon content is <2 wt.%, further preferably the regenerated catalyst carbon content is <0.5 wt.%.
In a preferred embodiment, the spent catalyst carbon content is 5-12 wt.%, and further preferably, the spent catalyst carbon content is 5-10 wt.%.
In a preferred embodiment, the turbulent fluidized bed reactor (1) has reaction zone reaction conditions of: the apparent linear velocity of the gas is 0.1-2m/s, the reaction temperature is 300-550 ℃, the reaction pressure is 100-500kPa, and the bed density is 200-1200kg/m3。
In a preferred embodiment, the catalytic cracking riser (28) reaction conditions are: the apparent linear velocity of the gas is 2.0-10.0m/s, the reaction temperature is 400-750 ℃, the reaction pressure is 100-500kPa, and the bed density is 30-300kg/m3。
In a preferred embodiment, the fluidized bed regenerator (14) regeneration zone reaction conditions are: the apparent linear velocity of the gas is 0.1-2m/s, the regeneration temperature is 500-750 ℃, the regeneration pressure is 100-500kPa, and the bed density is 200-1200kg/m3。
In a preferred embodiment, the oxygenate is methanol and/or dimethyl ether; and/or the regeneration medium is any one or a mixture of any several of air, oxygen-deficient air or water vapor; and/or the reactor stripping gas, the regenerator stripping gas, the spent stripping gas and the regenerated stripping gas are water vapor or nitrogen.
Drawings
Fig. 1 is a schematic diagram of an apparatus for producing propylene and C4 hydrocarbons from oxygenates according to one embodiment of the invention.
The reference numerals in the drawings are explained below:
1-turbulent fluidized bed reactor; 2-a reactor shell; 3-a reactor feed distributor (3-1 to 3-n); 4-reactor gas-solid separator 1; 5-reactor gas-solid separator 2; 6-reactor heat extractor; 7-product gas outlet; 8-reactor stripper; 9-reactor stripping gas inlet; 10-a to-be-grown inclined pipe; 11-spent spool valve; 12-a spent riser; 13-a spent lift gas inlet; 14-a fluidized bed regenerator; 15-a regenerator housing; 16-a regenerator feed distributor; 17-regenerator gas-solid separator; 18-regenerator heat extractor; 19-a flue gas outlet; 20-a regenerator stripper; 21-a regenerator stripping gas inlet; 22-regeneration inclined tube; 23-a regenerative slide valve; 24-a regenerative riser; 25-a regeneration lift gas inlet; 26-catalytic cracking inclined tube; 27-a catalytic cracking slide valve; 28-a catalytic cracking riser; hydrocarbon inlet above 29-C5.
Detailed Description
In one embodiment, the process for preparing propylene, C4 hydrocarbons from oxygenates and the apparatus thereof according to the present invention are schematically illustrated in fig. 1, the apparatus comprising:
a) a turbulent fluidized bed reactor (1) which comprises a reactor shell (2), n reactor feeding distributors (3-1-3-n), a reactor gas-solid separator (1), (4), a reactor gas-solid separator (2), (5), a reactor heat collector (6), a product gas outlet (7) and a reactor stripper (8), wherein the lower part of the turbulent fluidized bed reactor (1) is a reaction zone, the upper part of the turbulent fluidized bed reactor (1) is a settling zone, the n reactor feeding distributors (3-1-3-n) are arranged in the reaction zone from bottom to top, 0< n <10, the reactor heat collector (6) is arranged in the reaction zone, the reactor gas-solid separator (1), (4) and the reactor gas-solid separator (2), (5) are arranged outside the settling zone or the reactor shell (2), the inlet of the reactor gas-solid separator (1), (4) is connected with a regeneration riser (24), the catalyst outlet of the reactor gas-solid separator 1(4) is arranged at the bottom of the reaction zone, the gas outlet of the reactor gas-solid separator 1(4) is arranged in the settling zone, the inlet of the reactor gas-solid separator 2(5) is arranged in the settling zone, the catalyst outlet of the reactor gas-solid separator 2(5) is arranged in the reaction zone, the gas outlet of the reactor gas-solid separator 2(5) is connected with the product gas outlet (7), the inlet of the reactor stripper (8) is arranged in the reaction zone of the turbulent fluidized bed reactor (1), and the level of the inlet is higher than that of the reaction zone of 1/10;
b) a catalytic cracking riser (28), the bottom of which is provided with a hydrocarbon inlet (29) above C5, and the outlet of the catalytic cracking riser (28) is connected with the settling zone of the turbulent fluidized bed reactor (1); the inlet of the catalytic cracking riser (28) is connected with the outlet of the catalytic cracking inclined tube (26), a catalytic cracking slide valve (27) is arranged in the catalytic cracking inclined tube (26), and the inlet of the catalytic cracking inclined tube (26) is connected with the regenerator stripper (20).
c) A fluidized bed regenerator (14) comprising a regenerator housing (15), a regenerator feed distributor (16), a regenerator gas-solid separator (17), a regenerator heat remover (18), a flue gas outlet (19) and a regenerator stripper (20), the lower part of the fluidized bed regenerator (14) is a regeneration zone, the upper part of the fluidized bed regenerator (14) is a settling zone, a regenerator feed distributor (16) is arranged at the bottom of the regeneration zone, a regenerator heat extractor (18) is arranged in the regeneration zone, a regenerator gas-solid separator (17) is arranged outside the settling zone or a regenerator shell (15), an inlet of the regenerator gas-solid separator (17) is arranged in the settling zone, a catalyst outlet of the regenerator gas-solid separator (17) is arranged in the regeneration zone, a gas outlet of the regenerator gas-solid separator (17) is connected with a flue gas outlet (19), and an inlet of a regenerator stripper (20) is connected with the bottom of the regenerator shell (15);
d) the bottom of a reactor stripper (8) is provided with a reactor stripping gas inlet (9), the bottom of the reactor stripper (8) is connected with the inlet of a to-be-regenerated inclined pipe (10), a to-be-regenerated slide valve (11) is arranged in the to-be-regenerated inclined pipe (10), the outlet of the to-be-regenerated inclined pipe (10) is connected with the inlet of a to-be-regenerated lifting pipe (12), the bottom of the to-be-regenerated lifting pipe (12) is provided with a to-be-regenerated lifting gas inlet (13), and the outlet of the to-be-regenerated lifting pipe (12) is connected with the settling section of a fluidized bed regenerator (14);
e) the bottom of the regenerator stripper (20) is provided with a regenerator stripping gas inlet (21), the bottom of the regenerator stripper (20) is connected with the inlet of a regeneration inclined tube (22), a regeneration slide valve (23) is arranged in the regeneration inclined tube (22), the outlet of the regeneration inclined tube (22) is connected with the inlet of a regeneration lifting tube (24), the bottom of the regeneration lifting tube (24) is provided with a regeneration lifting gas inlet (25), and the outlet of the regeneration lifting tube (24) is connected with the inlet of a reactor gas-solid separator 1 (4).
In the above embodiments, the fluidized bed regenerator (14) may be a turbulent fluidized bed regenerator; the reactor gas-solid separators 1(4), the reactor gas-solid separators 2(5), and the regenerator gas-solid separator (17) may be cyclones.
In one embodiment, the process for producing propylene, C4 hydrocarbons from oxygenates of the present invention comprises:
a) introducing a raw material containing oxygen-containing compounds into a reaction zone of a turbulent fluidized bed reactor (1) from n reactor feeding distributors (3-1-3-n), and contacting the raw material with a catalyst to generate a material flow containing propylene and C4 hydrocarbon products and a carbon-containing spent catalyst;
b) sending a stream containing propylene and C4 hydrocarbon products flowing out of the turbulent fluidized bed reactor (1) into a product separation system, and separating to obtain propylene, C4 hydrocarbons, light components, propane and hydrocarbons above C5, wherein the light components contain more than 90 wt% of ethylene and small amounts of methane, ethane, hydrogen, CO and CO270-98 wt.% of light components are returned to the reaction zone of the turbulent fluidized bed reactor (1) from the reactor feeding distributor (3-1) at the bottom of the turbulent fluidized bed reactor (1), and the ethylene and the oxygen-containing compounds are subjected to alkylation reaction under the action of the catalyst to produce propylene and the likeLess than 30 wt.% of the light components are recovered as by-products;
c) more than 80 wt.% of the hydrocarbons with more than C5 from the separation system enter a catalytic cracking riser (28) from a hydrocarbon inlet (29) with more than C5 and are in concurrent contact with regenerated catalyst from a catalytic cracking inclined tube (26) to carry out cracking reaction to generate a stream containing propylene and C4 hydrocarbons and carbon-containing catalyst, then the stream containing propylene and C4 hydrocarbons and the carbon-containing catalyst enter a settling zone of the turbulent fluidized bed reactor (1) through an outlet of the catalytic cracking riser (28), and less than 20 wt.% of the hydrocarbons with more than C5 are recovered as byproducts;
d) the spent catalyst enters a settling section of a fluidized bed regenerator (14) through a reactor stripper (8), a spent inclined tube (10), a spent slide valve (11) and a spent riser (12);
e) introducing a regeneration medium into a regeneration zone of a fluidized bed regenerator (14) from a regenerator feed distributor (16), and carrying out a carbon burning reaction on the regeneration medium and a spent catalyst to generate a catalyst containing CO and CO2The flue gas and the regenerated catalyst are discharged after being dedusted by a gas-solid separator (17) of the regenerator;
f) a part of regenerated catalyst enters an inlet of a gas-solid separator 1(4) of the reactor through a regenerator stripper (20), a regeneration inclined tube (22), a regeneration slide valve (23) and a regeneration lifting tube (24), and after gas-solid separation, the regenerated catalyst enters the bottom of a reaction zone in the turbulent fluidized bed reactor (1); the other part of the regenerated catalyst enters a catalytic cracking riser (28) through a regenerator stripper (20), a catalytic cracking inclined tube (26) and a catalytic cracking slide valve (27);
g) the reactor stripping gas enters a reactor stripper (8) from a reactor stripping gas inlet (9) to be in countercurrent contact with the spent catalyst, and then enters a turbulent fluidized bed reactor (1); spent lifting gas enters a spent lifting pipe (12) from a spent lifting gas inlet (13) to be in concurrent flow contact with a spent catalyst, and then enters a settling section of a fluidized bed regenerator (14);
h) the regenerator stripping gas enters a regenerator stripper (20) from a regenerator stripping gas inlet (21) to be in countercurrent contact with the regenerated catalyst and then enters a fluidized bed regenerator (14); the regenerated lift gas enters a regenerated lift pipe (24) from a regenerated lift gas inlet (25) to be contacted with the regenerated catalyst in a concurrent flow manner, and then enters an inlet of a gas-solid separator 1(4) of the reactor.
To better illustrate the invention and to facilitate the understanding of the technical solutions thereof, the comparative examples and typical but non-limiting examples of the invention are as follows:
example 1
In this case, the comparative example, in which the apparatus shown in FIG. 1 was used, but the reactor gas-solid separator 1(4) was not included in the turbulent fluidized-bed reactor (1), and the regeneration riser (24) was directly connected to the settling zone of the turbulent fluidized-bed reactor (1).
The turbulent fluidized bed reactor (1) comprises 3 reactor feeding distributors (3-1-3), a reactor gas-solid separator (1) (4) is arranged outside a reactor shell (2), and the horizontal height of an inlet of a reactor stripper (8) is at the height of an 1/2 reaction zone. The reaction conditions of the reaction zone of the turbulent fluidized bed reactor (1) are as follows: the superficial linear velocity of the gas is about 1.0m/s, the reaction temperature is about 450 ℃, the reaction pressure is about 150kPa, and the bed density is about 350kg/m3。
The reaction conditions of the catalytic cracking riser (28) are as follows: the superficial linear velocity of the gas was about 5.0m/s, the reaction temperature was about 600 ℃, the reaction pressure was about 150kPa, and the bed density was about 50kg/m3。
The reaction conditions of the regeneration zone of the fluidized bed regenerator (14) are as follows: the gas superficial linear velocity is about 1.0m/s, the regeneration temperature is about 650 ℃, the regeneration pressure is about 150kPa, and the bed density is about 350kg/m3。
The catalyst contained SAPO molecular sieve, the spent catalyst had a carbon content of about 7% and the regenerated catalyst had a carbon content of about 0.2 wt.%.
The oxygen-containing compound is methanol, and the regeneration medium is air; the reactor stripping gas, the regenerator stripping gas, the to-be-generated lifting gas and the regeneration lifting gas are water vapor.
The light components were recycled in an amount of 20 wt.% of the methanol feed, and 71 wt.% of the light components were recycled in the system. The hydrocarbon above C5 is recycled in an amount of 12 wt.% of the methanol feed, and 92 wt.% of the hydrocarbon above C5 is recycled in the system.
Of product gas discharged from a turbulent fluidized-bed reactor (1)Comprises the following components: 31 wt.% propylene, 19 wt.% C4 hydrocarbons, 29 wt.% lights, 2 wt.% propane and 19 wt.% hydrocarbons above C5. The light fraction contained 98 wt.% ethylene and 2 wt.% methane, ethane, hydrogen, CO2And the like.
The composition of the product gas discharged by the separation system is: 50 wt.% propylene, 31 wt.% C4 hydrocarbons, 14 wt.% light components, 3 wt.% propane and 2 wt.% hydrocarbons above C5.
Example 2
By adopting the device shown in the figure 1, the turbulent fluidized bed reactor (1) comprises 3 reactor feeding distributors (3-1-3), a reactor gas-solid separator 1(4) is arranged outside a reactor shell (2), and the horizontal height of the inlet of a reactor stripper (8) is at the height of a 1/2 reaction zone. The reaction conditions of the reaction zone of the turbulent fluidized bed reactor (1) are as follows: the superficial linear velocity of the gas is about 1.0m/s, the reaction temperature is about 450 ℃, the reaction pressure is about 150kPa, and the bed density is about 350kg/m3。
The reaction conditions of the catalytic cracking riser (28) are as follows: the superficial linear velocity of the gas was about 5.0m/s, the reaction temperature was about 600 ℃, the reaction pressure was about 150kPa, and the bed density was about 50kg/m3。
The reaction conditions of the regeneration zone of the fluidized bed regenerator (14) are as follows: the gas superficial linear velocity is about 1.0m/s, the regeneration temperature is about 650 ℃, the regeneration pressure is about 150kPa, and the bed density is about 350kg/m3。
The catalyst contained SAPO molecular sieve, the spent catalyst had a carbon content of about 7% and the regenerated catalyst had a carbon content of about 0.2 wt.%.
The oxygen-containing compound is methanol, and the regeneration medium is air; the reactor stripping gas, the regenerator stripping gas, the to-be-generated lifting gas and the regeneration lifting gas are water vapor.
The light components were recycled in an amount of 15 wt.% of the methanol feed, and 98 wt.% of the light components were recycled in the system. The hydrocarbon above C5 is recycled in an amount of 12 wt.% of the methanol feed, and 92 wt.% of the hydrocarbon above C5 is recycled in the system.
The composition of the product gas discharged from the turbulent fluidized bed reactor (1) was: 35 wt.% propylene, 23 wt.% C4 hydrocarbons, 21 wt.% lights, 2 wt.% propane and so onAnd 19 wt.% hydrocarbons above C5. The light component contained 97 wt.% ethylene and 3 wt.% methane, ethane, hydrogen, CO2And the like.
The composition of the product gas discharged by the separation system is: 57 wt.% propylene, 37 wt.% C4 hydrocarbons, 1 wt.% lights, 3 wt.% propane, and 2 wt.% hydrocarbons above C5.
The only difference between this case and example 1 (comparative) is that the regenerated catalyst enters the bottom of the turbulent fluidized bed reactor and is first contacted with the light fraction, whereas the regenerated catalyst in example 1 enters the settling zone of the turbulent fluidized bed reactor. Comparing this case with example 1, it can be seen that the conversion rate of the light component can be greatly increased by contacting the light component with the catalyst first, and the light component discharged from the separation system in this case is only 7% of that in the comparative case, so the apparatus of the present invention effectively increases the reaction rate of the vinyl alkylation.
Example 3
This case is a comparative case, using the apparatus shown in FIG. 1, but without the catalytic cracking ramp (26), catalytic cracking slide valve (27) and catalytic cracking riser (28). The hydrocarbons above C5 are not recycled and are directly recovered as by-products.
The turbulent fluidized bed reactor (1) comprises 4 reactor feeding distributors (3-1-3-4), a reactor gas-solid separator (1) (4) is arranged in a settling zone, and the horizontal height of an inlet of a reactor stripper (8) is at the height of 3/4 reaction zones. The reaction conditions of the reaction zone of the turbulent fluidized bed reactor (1) are as follows: the superficial linear velocity of the gas is about 1.2m/s, the reaction temperature is about 360 ℃, the reaction pressure is about 200kPa, and the bed density is about 300kg/m3。
The reaction conditions of the regeneration zone of the fluidized bed regenerator (14) are as follows: the gas superficial linear velocity is about 1.2m/s, the regeneration temperature is about 700 ℃, the regeneration pressure is about 200kPa, and the bed density is about 300kg/m3。
The catalyst contains SAPO molecular sieve, the carbon content of the spent catalyst is about 8 percent, and the carbon content of the regenerated catalyst is about 0.1 percent by weight.
The oxygen-containing compound is methanol, and the regeneration medium is air; the reactor stripping gas, the regenerator stripping gas, the to-be-generated lifting gas and the regeneration lifting gas are water vapor.
The light components were recycled in an amount of 16 wt.% of the methanol feed, and 90 wt.% of the light components were recycled in the system.
The composition of the product gas discharged from the turbulent fluidized bed reactor (1) was: 39 wt.% propylene, 25 wt.% C4 hydrocarbons, 29 wt.% lights, 2 wt.% propane and 5 wt.% hydrocarbons above C5. The light component contains 96 wt.% of ethylene and 4 wt.% of methane, ethane, hydrogen, CO2And the like.
The composition of the product gas discharged by the separation system is: 53 wt.% propylene, 33 wt.% C4 hydrocarbons, 4 wt.% lights, 3 wt.% propane and 7 wt.% hydrocarbons above C5.
Example 4
By adopting the device shown in the figure 1, the turbulent fluidized bed reactor (1) comprises 4 reactor feeding distributors (3-1-3-4), the reactor gas-solid separator 1(4) is arranged in a settling zone, and the horizontal height of the inlet of the reactor stripper (8) is at the height of 3/4 reaction zone. The reaction conditions of the reaction zone of the turbulent fluidized bed reactor (1) are as follows: the superficial linear velocity of the gas is about 1.2m/s, the reaction temperature is about 360 ℃, the reaction pressure is about 200kPa, and the bed density is about 300kg/m3。
The reaction conditions of the catalytic cracking riser (28) are as follows: the superficial linear velocity of the gas is about 7.0m/s, the reaction temperature is about 650 ℃, the reaction pressure is about 200kPa, and the bed density is about 40kg/m3。
The reaction conditions of the regeneration zone of the fluidized bed regenerator (14) are as follows: the gas superficial linear velocity is about 1.2m/s, the regeneration temperature is about 700 ℃, the regeneration pressure is about 200kPa, and the bed density is about 300kg/m3。
The catalyst contains SAPO molecular sieve, the carbon content of the spent catalyst is about 8 percent, and the carbon content of the regenerated catalyst is about 0.1 percent by weight.
The oxygen-containing compound is methanol, and the regeneration medium is air; the reactor stripping gas, the regenerator stripping gas, the to-be-generated lifting gas and the regeneration lifting gas are water vapor.
The light components were recycled in an amount of 16 wt.% of the methanol feed, and 90 wt.% of the light components were recycled in the system. The hydrocarbon above C5 is recycled in an amount of 4 wt.% based on the methanol feed, and 95 wt.% of the hydrocarbon above C5 is recycled in the system.
The composition of the product gas discharged from the turbulent fluidized bed reactor (1) was: 34 wt.% propylene, 23 wt.% C4 hydrocarbons, 25 wt.% light components, 2 wt.% propane and 16 wt.% hydrocarbons above C5. The light component contains 96 wt.% of ethylene and 4 wt.% of methane, ethane, hydrogen, CO2And the like.
The composition of the product gas discharged by the separation system is: 55 wt.% propylene, 37 wt.% C4 hydrocarbons, 4 wt.% lights, 3 wt.% propane, and 1 wt.% hydrocarbons above C5.
The only difference between this case and example 3 (comparative) is the recycle of hydrocarbons above C5. Comparing this case with example 3, it can be seen that the hydrocarbon above C5 discharged from the separation system in this case is only 14% of the comparative case, therefore, the apparatus of the present invention can effectively catalyze the cracking of the hydrocarbon above C5 into propylene and C4 hydrocarbon.
Example 5
By adopting the device shown in the figure 1, the turbulent fluidized bed reactor (1) comprises 6 reactor feeding distributors (3-1-3-6), the reactor gas-solid separator 1(4) is arranged in a settling zone, and the horizontal height of the inlet of the reactor stripper (8) is at the height of 5/6 reaction zone. The reaction conditions of the reaction zone of the turbulent fluidized bed reactor (1) are as follows: the gas superficial linear velocity is about 1.5m/s, the reaction temperature is about 420 ℃, the reaction pressure is about 250kPa, and the bed density is about 250kg/m3。
The reaction conditions of the catalytic cracking riser (28) are as follows: the superficial linear velocity of the gas is about 7.0m/s, the reaction temperature is about 700 ℃, the reaction pressure is about 250kPa, and the bed density is about 40kg/m3。
The reaction conditions of the regeneration zone of the fluidized bed regenerator (14) are as follows: the gas apparent linear velocity is about 1.5m/s, the regeneration temperature is about 700 ℃, the regeneration pressure is about 250kPa, and the bed density is about 250kg/m3。
The catalyst contained SAPO molecular sieve, spent catalyst carbon content was about 9% and regenerated catalyst carbon content was about 0.05 wt.%.
The oxygen-containing compound is dimethyl ether, and the regeneration medium is oxygen-poor air; the reactor stripping gas, the regenerator stripping gas, the to-be-generated lifting gas and the regeneration lifting gas are nitrogen.
The light components were recycled in an amount of 19 wt.% of the dimethyl ether feed and 85 wt.% of the light components were recycled in the system. The above-C5 hydrocarbons are recycled in an amount of 14 wt.% based on the dimethyl ether feed, and 90 wt.% of above-C5 hydrocarbons are recycled in the system.
The composition of the product gas discharged from the turbulent fluidized bed reactor (1) was: 35 wt.% propylene, 23 wt.% C4 hydrocarbons, 23 wt.% light components, 3 wt.% propane and 16 wt.% hydrocarbons above C5. The light component contains 96 wt.% of ethylene and 4 wt.% of methane, ethane, hydrogen, CO2And the like.
The composition of the product gas discharged by the separation system is: 53 wt.% propylene, 35 wt.% C4 hydrocarbons, 5 wt.% lights, 5 wt.% propane and 2 wt.% hydrocarbons above C5.
The present invention has been described in detail above, but the present invention is not limited to the specific embodiments described herein. It will be understood by those skilled in the art that other modifications and variations may be made without departing from the scope of the invention. The scope of the invention is defined by the appended claims.
Claims (12)
1. An apparatus for the production of propylene and C4 hydrocarbons from oxygenates, the apparatus comprising:
a turbulent fluidized bed reactor, which comprises a reactor shell, n reactor feeding distributors, n is more than or equal to 3 and less than 10, a reactor gas-solid separator 1, a reactor gas-solid separator 2, a reactor heat extractor, a product gas outlet and a reactor stripper, wherein the lower part of the turbulent fluidized bed reactor is a reaction zone, the upper part of the turbulent fluidized bed reactor is a settling zone, the n reactor feeding distributors are arranged in the reaction zone from bottom to top, the main component is light ethylene component, oxygen-containing compounds enter from the lowermost reactor feeding distributor, oxygen-containing compounds enter from the n reactor feeding distributors respectively, regenerated catalysts directly enter the bottom of the reaction zone, the reactor heat extractor is arranged in the reaction zone, the reactor gas-solid separator 1 and the reactor gas-solid separator 2 are arranged in the settling zone or outside the reactor shell, an inlet of the reactor gas-solid separator 1 is connected with a regeneration riser, the catalyst outlet of the reactor gas-solid separator 1 is arranged at the bottom of the reaction zone, the gas outlet of the reactor gas-solid separator 1 is arranged in the settling zone, the inlet of the reactor gas-solid separator 2 is arranged in the settling zone, the catalyst outlet of the reactor gas-solid separator 2 is arranged in the reaction zone, the gas outlet of the reactor gas-solid separator 2 is connected with the product gas outlet, the reactor stripper penetrates through the reactor shell from outside to inside at the bottom of the turbulent fluidized bed reactor and opens in the reaction zone of the turbulent fluidized bed reactor, and the horizontal height of the opening of the reactor stripper in the reactor shell is higher than the height of the 1/10 reaction zone and is less than or equal to the height of the 5/6 reaction zone;
the bottom of the catalytic cracking riser is connected with the outlet of the catalytic cracking inclined tube and is provided with a hydrocarbon inlet more than C5, and the outlet of the catalytic cracking riser is connected with the settling zone of the turbulent fluidized bed reactor;
the fluidized bed regenerator comprises a regenerator shell, a regenerator feeding distributor, a regenerator gas-solid separator, a regenerator heat extractor, a flue gas outlet and a regenerator stripper, wherein the lower part of the fluidized bed regenerator is a regeneration zone, the upper part of the fluidized bed regenerator is a settling zone, the regenerator feeding distributor is arranged at the bottom of the regeneration zone, the regenerator heat extractor is arranged in the regeneration zone, the regenerator gas-solid separator is arranged outside the settling zone or the regenerator shell, an inlet of the regenerator gas-solid separator is arranged in the settling zone, a catalyst outlet of the regenerator gas-solid separator is arranged in the regeneration zone, a gas outlet of the regenerator gas-solid separator is connected with the flue gas outlet, and the regenerator stripper is opened at the bottom of the regenerator shell;
the bottom of the reactor stripper is provided with a reactor stripping gas inlet, the bottom of the reactor stripper is connected with the inlet of a to-be-regenerated inclined pipe, a to-be-regenerated slide valve is arranged in the to-be-regenerated inclined pipe, the outlet of the to-be-regenerated inclined pipe is connected with the inlet of a to-be-regenerated lifting pipe, the bottom of the to-be-regenerated lifting pipe is provided with a to-be-regenerated lifting gas inlet, and the outlet of the to-be-regenerated lifting pipe is connected with the settling section of the fluidized bed regenerator;
the bottom of the regenerator stripper is provided with a regenerator stripping gas inlet, the bottom of the regenerator stripper is connected with the inlet of a regeneration inclined pipe, a regeneration slide valve is arranged in the regeneration inclined pipe, the outlet of the regeneration inclined pipe is connected with the inlet of a regeneration riser pipe, the bottom of the regeneration riser pipe is provided with a regeneration lifting gas inlet, and the outlet of the regeneration riser pipe is connected with the inlet of the reactor gas-solid separator 1;
the bottom of the regenerator stripper is also connected to the inlet of a catalytic cracking inclined tube, and a catalytic cracking slide valve is arranged in the catalytic cracking inclined tube.
2. The apparatus of claim 1 wherein the catalytic cracking riser and the turbulent fluidized bed reactor share a gas-solid separator 2.
3. The apparatus of claim 1, wherein the fluidized bed regenerator is a turbulent fluidized bed regenerator.
4. The apparatus of claim 1 wherein the reactor gas-solid separator 1, reactor gas-solid separator 2 and regenerator gas-solid separator are cyclones.
5. A process for producing propylene and C4 hydrocarbons from oxygenates comprising:
introducing an oxygen-containing compound into a reaction zone of a turbulent fluidized bed reactor from n reactor feeding distributors, and contacting the oxygen-containing compound with a catalyst to generate a material flow containing propylene and C4 hydrocarbon products and a carbon-containing spent catalyst, wherein the n reactor feeding distributors are arranged in the reaction zone from bottom to top, and n is more than or equal to 3 and less than 10;
the spent catalyst is regenerated by a fluidized bed regenerator to form a regenerated catalyst, one part of the regenerated catalyst enters the bottom of a reaction zone in the turbulent fluidized bed reactor after being subjected to gas-solid separation by a gas-solid separator 1 of the reactor, and the other part of the regenerated catalyst enters a catalytic cracking riser through a catalytic cracking inclined tube;
sending a stream containing propylene and C4 hydrocarbon products flowing out of the turbulent fluidized bed reactor into a product separation system, and separating to obtain propylene, C4 hydrocarbons, light components, propane and hydrocarbons above C5, wherein the light components contain more than 90 wt% of ethylene and a small amount of methane,Ethane, Hydrogen, CO and CO2More than 70 wt.% of the light components are returned to the reaction zone of the turbulent fluidized bed reactor from the lowermost reactor feed distributor of the turbulent fluidized bed reactor, the ethylene and the oxygenate are alkylated with the catalyst to produce a product comprising propylene, and the propylene produced is alkylated, less than 30 wt.% of the light components being recovered as by-products;
more than 80 wt.% of the hydrocarbons with more than C5 from the separation system enter the catalytic cracking riser from the hydrocarbon inlet with more than C5 and are in concurrent contact with the regenerated catalyst from the catalytic cracking inclined tube, so that a cracking reaction is carried out, a stream containing propylene and C4 hydrocarbons and a carbon-containing catalyst are generated, then the stream containing propylene and C4 hydrocarbons and the carbon-containing catalyst enter a settling zone of the turbulent fluidized bed reactor through the outlet of the catalytic cracking riser, and less than 20 wt.% of the hydrocarbons with more than C5 are recovered as a byproduct,
wherein the method is performed using the apparatus of any one of claims 1 to 4.
6. The method of claim 5, wherein
The spent catalyst enters a settling section of a fluidized bed regenerator through a reactor stripper, a spent inclined tube, a spent slide valve and a spent riser;
introducing the regenerated medium into the regeneration zone of the fluidized bed regenerator from the regenerator feeding distributor, and performing a carbon burning reaction on the regenerated medium and the spent catalyst to generate a catalyst containing CO and CO2The flue gas and the regenerated catalyst are discharged after being dedusted by a gas-solid separator of the regenerator;
a part of regenerated catalyst enters an inlet of a reactor gas-solid separator 1 through a regenerator stripper, a regeneration inclined pipe, a regeneration slide valve and a regeneration lifting pipe, and after gas-solid separation, the regenerated catalyst enters the bottom of a reaction zone in the turbulent fluidized bed reactor; the other part of the regenerated catalyst enters a catalytic cracking riser through a regenerator stripper, a catalytic cracking inclined tube and a catalytic cracking slide valve;
the reactor stripping gas enters a reactor stripper from a reactor stripping gas inlet to be in countercurrent contact with the spent catalyst, and then enters the turbulent fluidized bed reactor; the spent lifting gas enters a spent lifting pipe from a spent lifting gas inlet to be in concurrent contact with a spent catalyst and then enters a settling section of a fluidized bed regenerator;
the regenerator stripping gas enters a regenerator stripper from a regenerator stripping gas inlet to be in countercurrent contact with the regenerated catalyst and then enters a fluidized bed regenerator; the regenerated lift gas enters the regenerated lift pipe from the regenerated lift gas inlet to be in concurrent contact with the regenerated catalyst and then enters the inlet of the reactor gas-solid separator 1.
7. The method of claim 5, wherein the catalyst contains a SAPO molecular sieve.
8. The process of claim 5, wherein the lights recycle is from 5 to 40 wt.% of the oxygenate feed.
9. The process of claim 5 wherein the C5 plus hydrocarbon recycle is from 2 to 20 wt.% of the oxygenate feed.
10. The process of claim 5, wherein the spent catalyst carbon content is 5-12 wt.% and the regenerated catalyst carbon content is <2 wt.%.
11. The process of claim 5, wherein the oxygenate is methanol and/or dimethyl ether; and/or the regeneration medium is any one or a mixture of any several of air, oxygen-deficient air or water vapor; and/or the reactor stripping gas, the regenerator stripping gas, the spent stripping gas and the regenerated stripping gas are water vapor or nitrogen.
12. The process of claim 5 wherein the turbulent fluidized bed reactor reaction zone reaction conditions are: the apparent linear velocity of the gas is 0.1-2m/s, the reaction temperature is 300-550 ℃, the reaction pressure is 100-500kPa, and the bed density is 200-1200kg/m3(ii) a And/or the catalytic cracking riser reactionThe conditions are as follows: the apparent linear velocity of the gas is 2.0-10.0m/s, the reaction temperature is 400-750 ℃, the reaction pressure is 100-500kPa, and the bed density is 30-300kg/m3(ii) a And/or the reaction conditions in the regeneration zone of the fluidized bed regenerator are as follows: the apparent linear velocity of the gas is 0.1-2m/s, the regeneration temperature is 500-750 ℃, the regeneration pressure is 100-500kPa, and the bed density is 200-1200kg/m3。
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