CN116020357A - Cyclone reactor and method for producing low-carbon olefin - Google Patents
Cyclone reactor and method for producing low-carbon olefin Download PDFInfo
- Publication number
- CN116020357A CN116020357A CN202111243064.0A CN202111243064A CN116020357A CN 116020357 A CN116020357 A CN 116020357A CN 202111243064 A CN202111243064 A CN 202111243064A CN 116020357 A CN116020357 A CN 116020357A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- cyclone
- cyclone chamber
- gas
- product gas
- 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.)
- Pending
Links
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title abstract description 20
- 239000003054 catalyst Substances 0.000 claims abstract description 170
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 36
- 150000001336 alkenes Chemical class 0.000 claims abstract description 12
- 230000002093 peripheral effect Effects 0.000 claims abstract description 7
- 238000006243 chemical reaction Methods 0.000 claims description 44
- 239000002994 raw material Substances 0.000 claims description 23
- 238000000034 method Methods 0.000 claims description 12
- 230000008569 process Effects 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 6
- 230000004323 axial length Effects 0.000 claims description 6
- 230000008021 deposition Effects 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 5
- 230000007704 transition Effects 0.000 claims description 5
- 230000000903 blocking effect Effects 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 238000006555 catalytic reaction Methods 0.000 abstract description 7
- 230000035484 reaction time Effects 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 130
- 238000007599 discharging Methods 0.000 description 12
- 239000012071 phase Substances 0.000 description 11
- 239000007787 solid Substances 0.000 description 11
- 230000009471 action Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 239000007921 spray Substances 0.000 description 6
- 239000007806 chemical reaction intermediate Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 239000007790 solid phase Substances 0.000 description 3
- 238000013461 design Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- -1 ethylene, propylene Chemical group 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 238000007363 ring formation reaction Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
Images
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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to the field of production of olefins from methanol and discloses a cyclone reactor and a production method of low-carbon olefins, wherein the cyclone reactor comprises a body with two closed ends and a drainage tube coaxially arranged in a cyclone chamber, the cyclone chamber is formed in the body, a catalyst feed port, a discharge port and a raw gas inlet are arranged on the peripheral wall of the cyclone chamber, the cyclone reactor is arranged at the downstream of the feed direction of the catalyst feed port, so that a catalyst entering the cyclone chamber from the catalyst feed port flows to a catalyst discharge port along the inner wall surface of the cyclone chamber under the pushing of the raw gas, the raw gas generates product gas through catalytic reaction, and a product gas outlet is arranged on the end wall of the body, which is close to one end of the catalyst feed port; the tube wall of the drainage tube is provided with an arc surface opening for product gas in the cyclone chamber to enter the drainage tube. The utility model solves the technical problem that the reaction time cannot be further shortened due to the influence of the reactor form, so that the selection of the low-carbon olefin is difficult to be further improved.
Description
Technical Field
The utility model relates to the field of production of olefins from methanol, in particular to a cyclone reactor and a production method of low-carbon olefins.
Background
The technology for producing low-carbon olefins such as ethylene, propylene and the like by methanol under the action of a catalyst is proved to be completely suitable for producing products such as polyolefin and the like.
At present, industrial application of the domestic methanol-to-olefin (MTO) technology is on scale, 75% of domestic olefin products are still produced by a crude oil route from the market share, and the ratio of coal-to-olefin to methanol-to-olefin is about 17%. Along with the continuous establishment and production of a plurality of domestic coal-to-olefin projects, the competition among the existing MTO technology is extremely intense, the international oil price continuously fluctuates, and the fluidized bed reactor is used as the most core device of the whole coal-to-olefin project, so that the methanol-to-olefin process technology needs to be widely and deeply researched and innovated.
In the process of converting MTO reaction into hydrocarbon, the methanol can go through the step of methanol to reaction intermediate, the generated reaction intermediate is mainly polymethylbenzene, the reaction rate of converting the reaction intermediate into olefin is very fast, and then the low-carbon olefin product is subjected to a series of polymerization, cyclization and hydrogen transfer processes to form C4 and C5 and above products. At present, the gas-solid contact time of the MTO technology is 2-8 seconds, and according to the mechanism, if the reaction progress can be effectively controlled and the reaction process can be rapidly stopped in a shorter time, the selectivity of the MTO reaction for low-carbon olefin can be further improved.
CN205024117 discloses an utility model patent of a reaction apparatus for preparing olefin from methanol, said utility model adopts a dense-phase fluidized bed reactor with transverse grating at bottom, and said apparatus can break bubbles to enhance gas-solid mixing, and can shorten upper free space of reaction apparatus and reduce gas-solid reaction time, so as to raise product selectivity and olefin yield. According to the patent, the gas reaction residence time of the methanol-to-olefin reaction equipment can be shortened to 1-2 s.
CN104437274 discloses an utility model patent of a dense-phase fluidized bed reactor for preparing olefin by methanol conversion, the patent uses a specific gas pre-riser to extend into a bed layer of the dense-phase fluidized bed reactor, the gas is ventilated to the bed layer in radial direction, the gas-solid mixing condition in a single-pass reaction process can be greatly improved by combining with a special baffle design in the reactor, the selectivity of low-carbon olefin in the product is improved, and the residence time can be controlled within 0.5-1.5 s.
The two parts are still mainly used as a reactor by a fluidized bed commonly used at present, and the gas-solid contact mode of the reactor limits the gas-solid contact time to be difficult to further shorten by improving the gas-solid phase distribution in the reaction process and improving the selectivity of the low-carbon olefin in the reaction process.
CN207012952 discloses an utility model of an ultra-short contact fluidized bed reactor, which can be used in the reaction process of preparing olefin from MTO methanol, and the reactor mainly comprises a catalyst distribution pipe, a feed nozzle, a catalyst contact area, a settler and a gas/steam stripper, wherein the catalyst contact area is positioned at one side of the settler, the catalyst is vertically contacted with raw materials, the gas-solid initial contact time is short, and then interphase separation is completed through large-space sedimentation and an outlet gas-solid separator. The technology uses gas-solid vertical contact, greatly reduces the contact time of gas and solid phase in a catalyst contact zone, but the gas phase is seriously carried in the tiny process of the catalyst, a dispersion state is formed in a large space of a sedimentation zone, and the actual residence time of the gas phase finally leaving the reactor from a gas-solid separator is far longer than the fluidized bed time, so that after the initial gas-solid contact reaction, the gas phase further continues to undergo side reaction in the sedimentation zone.
The prior MTO reactor comprises a bubbling fluidized bed, a dense-phase fluidized bed, a rapid fluidized bed and other fluidization types and processes, but still has the problem that the selectivity of the low-carbon olefin is difficult to further improve.
Disclosure of Invention
The utility model aims to solve the technical problems that the reaction time cannot be further shortened and the selection of low-carbon olefin is difficult to further improve due to the influence of the reactor form of an MTO reactor in the prior art.
In order to achieve the above object, the present utility model provides, in one aspect, a cyclone reactor.
The cyclone reactor comprises:
the catalyst feeding device comprises a body, wherein the body is a cylinder body with two closed ends, a cyclone chamber for carrying out gas material reaction is formed in the body, a catalyst feeding hole, a catalyst discharging hole and a raw gas inlet are formed in the peripheral wall of the body, wherein the catalyst feeding hole and the catalyst discharging hole are respectively positioned at two axial ends of the body, the raw gas inlet and the catalyst feeding hole are positioned in the same circumferential direction of the body and are arranged at the downstream of the feeding direction of the catalyst feeding hole, so that a catalyst entering the cyclone chamber from the catalyst feeding hole is driven by raw gas to rotationally flow to the catalyst discharging hole along the inner wall surface of the cyclone chamber, the raw gas is subjected to catalytic reaction to generate product gas, and a product gas outlet is formed in the end wall of the body, which is close to one end of the catalyst feeding hole; and
the drainage tube is coaxially arranged in the cyclone chamber, one end of the drainage tube is connected with the product gas outlet, and a cambered surface opening for the product gas in the cyclone chamber to enter the drainage tube is formed in the tube wall of the drainage tube.
The utility model provides a cyclone reactor, which is provided with a cylindrical body with two closed ends, wherein a cyclone chamber for carrying out gas material reaction is formed in the body, a catalyst feed port, a catalyst discharge port and a raw gas inlet are arranged on the peripheral wall, the catalyst feed port and the catalyst discharge port are respectively positioned at two axial ends of the body, and the raw gas inlet and the catalyst feed port are arranged in the same axial direction and are arranged at the downstream of the feeding direction of the catalyst feed port, so that a catalyst entering the cyclone chamber at the catalyst feed port flows to the catalyst discharge port along the surface of the inner wall surface of the cyclone chamber under the pushing of raw gas, and the raw gas generates product gas through catalytic reaction. The arrangement of the structure strengthens the mass transfer process of the raw material gas and the catalyst by utilizing inertia and centrifugal force, improves the catalytic reaction efficiency, simultaneously, the utility model coaxially arranges the drainage tube with one end connected with the product gas outlet in the cyclone chamber, and the pipe wall is provided with the cambered surface opening for the product gas in the cyclone chamber to enter the interior of the cyclone chamber, so that the product gas generated by the catalytic reaction is pumped away under the action of inertia, the reaction process is further accelerated, and the technical problem that the reaction time cannot be further shortened due to the influence of the form of the reactor, and the selection of the low-carbon olefin is difficult to be further improved is solved.
Preferably, the cyclone reactor comprises a catalyst feeding pipe arranged at the catalyst feeding port and used for introducing catalyst into the cyclone chamber, and the catalyst feeding pipe comprises a straight pipe section arranged outside the cyclone chamber and an arc pipe section arranged on the inner wall surface of the cyclone chamber in a fitting manner.
Preferably, the included angle between the central line of the straight pipe section and the tangent line of the arc pipe section is alpha, wherein the value of alpha is 30-70 degrees.
Preferably, the opening direction of the arc opening is away from the catalyst feed inlet and the feed gas inlet in the radial direction of the body.
Preferably, the cambered surface opening comprises at least one of the following modes:
in a first mode, a plurality of cambered surface openings are formed, and the cambered surface openings are arranged at intervals along the axial direction of the drainage tube;
in the second mode, the opening size of the cambered surface opening in the circumferential direction is theta, wherein the value range of theta is 40-60 degrees.
Preferably, the product gas outlet is connected with a product gas outlet pipe, the diameter of the drainage pipe is larger than that of the product gas outlet pipe, and the drainage pipe is connected with the product gas outlet pipe through a conical transition section.
Preferably, the axial length L1 of the drainage tube is less than 4/5 of the axial length L0 of the cyclone chamber; and/or the size relation between the radius R2 of the drainage tube and the radius R1 of the cyclone chamber is 1/5R 1-R2-1/2R 1.
Preferably, the cyclone reactor further comprises a feed gas inlet distributor connected to the feed gas inlet for dispersing feed gas entering the cyclone chamber.
Preferably, the feed gas inlet distributor comprises a straight-through pipe and a plurality of spray pipes communicated with the straight-through pipe, wherein the spray pipes are arranged side by side along the inlet direction perpendicular to the straight-through pipe so as to split the feed gas in the straight-through pipe.
Preferably, the outlet end of the spray pipe is provided with a guide piece for guiding the raw material gas in the spray pipe to the direction of the catalyst discharge port of the cyclone chamber.
Preferably, the guide piece is a pipe with an inclined outlet end, and an included angle between the axial direction of the outlet end of the guide piece and the axial direction of the spray pipe is gamma, wherein the value of gamma is in the range of 0-60 degrees.
Preferably, a catalyst discharge slot for blocking the flow of the catalyst and gathering the catalyst is arranged at the catalyst discharge hole, and the catalyst discharge hole is arranged in the catalyst discharge slot.
Preferably, the catalyst discharging groove is of a funnel-shaped structure, and the catalyst discharging hole is arranged in the middle of the catalyst discharging groove; and/or the included angle between the central line of the catalyst discharge port and the vertical direction of the inlet direction of the raw material gas is phi, wherein the value range of phi is 0-45 degrees.
The second aspect of the utility model provides a method for producing light olefins.
The method for producing the low-carbon olefin adopts any one of the cyclone reactors.
Preferably, the reaction conditions of the production method include at least one scenario,
firstly, preheating raw material gas which enters the cyclone reactor and mainly contains methanol, wherein the preheating temperature is 100-200 ℃;
in a second scenario, the active component of the catalyst entering the cyclone reactor is a SAPO-34 molecular sieve; preferably, the catalyst has an average carbon deposition of 0.5wt% to 6wt%; further preferably, the catalyst has an average carbon deposition of 4wt% to 5wt%;
and in a third scenario, the reaction temperature in the cyclone chamber is 400-500 ℃ and the reaction pressure is 0.01-1 MPa.
Preferably, when the cyclone reactor comprises a feed gas inlet distributor, the gas velocity of the feed gas passing through an outlet nozzle of the feed gas inlet distributor is 10-30 m/s;
the reaction contact time of the raw material gas and the catalyst in the cyclone chamber is 0.1-2 s, preferably 0.2-0.5 s;
when the product gas outlet is connected with a product gas outlet pipe, the product gas is discharged from the cyclone reactor through the product gas outlet pipe, and the flow velocity of the product gas in the pipeline of the product gas outlet pipe is 10-20 m/s.
Drawings
FIG. 1 is a schematic view of the overall structure of a cyclone reactor provided by the utility model;
FIG. 2 is a schematic view of the H-H section structure of FIG. 1;
FIG. 3 is a schematic side elevational view of FIG. 1;
FIG. 4 is a schematic view of the h-h section structure of FIG. 3;
fig. 5 is a top structural perspective view of fig. 1.
Description of the reference numerals
1. A body; 101. a swirl chamber; 102. a catalyst feed port; 103. a catalyst discharge port; 104. a feed gas inlet; 105. a product gas outlet; 2. a catalyst feed tube; 201. a straight tube section; 202. an arc-shaped pipe section; 3. a catalyst discharge pipe; 4. a feed gas inlet distributor; 401. a straight pipe; 402. a spray pipe; 403. a guide member; 5. a drainage tube; 501. an arc surface opening; 6. a product gas outlet pipe; 7. a tapered transition section; 8. a catalyst discharge chute; a. a feed gas; b. product gas; c. a catalyst; d. a catalyst.
Detailed Description
In order that those skilled in the art will better understand the present utility model, a technical solution in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in which it is apparent that the described embodiments are only some embodiments of the present utility model, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present utility model without making any inventive effort, shall fall within the scope of the present utility model.
It should be noted that the terms "first," "second," and the like in the description and the claims of the present utility model and the above figures are used for distinguishing between similar objects and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used may be interchanged where appropriate in order to describe the embodiments of the utility model herein. Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.
In the present utility model, the terms "upper", "lower", "front", "rear", "inner", "outer", "middle", "vertical" and "horizontal", etc. indicate an azimuth or a positional relationship based on that shown in the drawings. These terms are only used to better describe the present utility model and its embodiments and are not intended to limit the scope of the indicated devices, elements or components to the particular orientations or to configure and operate in the particular orientations.
Also, some of the terms described above may be used to indicate other meanings in addition to orientation or positional relationships, for example, the term "upper" may also be used to indicate some sort of attachment or connection in some cases. The specific meaning of these terms in the present utility model will be understood by those of ordinary skill in the art according to the specific circumstances.
In addition, the term "plurality" shall mean two as well as more than two.
It should be noted that, without conflict, the embodiments of the present utility model and features of the embodiments may be combined with each other. The utility model will be described in detail below with reference to the drawings in connection with embodiments.
As shown in fig. 1 to 5, the present utility model provides a cyclone reactor that can be used for producing low-carbon olefin.
The cyclone reactor comprises a body 1 and a drainage tube 5, wherein the body 1 is a cylinder body with two closed ends, a cyclone chamber 101 for carrying out gas material reaction is formed in the body 1, a catalyst feed inlet 102, a catalyst discharge outlet 103 and a raw gas inlet 104 are arranged on the peripheral wall of the body 1, wherein the catalyst feed inlet 102 and the catalyst discharge outlet 103 are respectively positioned at the two axial ends of the body 1, the raw gas inlet 104 and the catalyst feed inlet 102 are positioned on the same circumferential direction of the body 1, and the raw gas inlet 104 is arranged at the downstream of the feed direction of the catalyst feed inlet 102, so that a catalyst c entering the cyclone chamber 101 from the catalyst feed inlet 102 flows to the catalyst discharge outlet 103 along the inner wall surface of the cyclone chamber 101 under the pushing of raw gas a, and the raw gas a generates a product gas b through the catalytic reaction. And a product gas outlet 105 is provided in the end wall of the body 1 near the end of the catalyst feed port 102.
The drainage tube 5 is coaxially arranged in the cyclone chamber 101, one end of the drainage tube 5 is connected with the product gas outlet 105, and a cambered surface opening 501 for the product gas b in the cyclone chamber 101 to enter the drainage tube 5 is arranged on the tube wall of the drainage tube 5.
The utility model provides a cyclone reactor, which is provided with a cylindrical body with two closed ends, wherein a cyclone chamber for carrying out gas material reaction is formed in the body, a catalyst feed inlet, a catalyst discharge outlet and a raw gas inlet are arranged on the peripheral wall, the catalyst feed inlet and the catalyst discharge outlet are respectively positioned at two axial ends of the body, and the raw gas inlet and the catalyst feed inlet are arranged to be positioned in the same circumferential direction and are arranged at the reverse downstream of the feed direction of the catalyst feed inlet, so that a catalyst entering the cyclone chamber at the catalyst feed inlet flows to the catalyst discharge outlet along the inner surface of the cyclone chamber under the pushing of raw gas, and the raw gas generates product gas through catalytic reaction. The arrangement of the structure improves the reaction efficiency of the raw material gas and the catalyst by utilizing inertia and centrifugal force, meanwhile, one end of the cyclone chamber is coaxially arranged in the cyclone chamber and is connected with the product gas outlet, and the tube wall is provided with the drainage tube for enabling the product gas obtained in the cyclone chamber to enter the cambered surface opening of the cyclone chamber, so that the product gas generated by the reaction is pumped away under the action of inertia, the reaction process is further accelerated, and the technical problem that the reaction time cannot be further shortened due to the influence of the form of the reactor, and the selection of the low-carbon olefin is difficult to be further improved is solved.
In an alternative embodiment of the present utility model, the cyclone reactor includes a catalyst feed pipe 2 provided at the catalyst feed port 102 for feeding catalyst into the cyclone chamber 101, the catalyst feed pipe 2 including a straight pipe section 201 provided outside the cyclone chamber 101 and an arc pipe section 202 provided to fit the inner wall surface of the cyclone chamber 101. In a further alternative embodiment of the present utility model, the centerline of the straight tube segment 201 is at an angle α to the tangent of the arcuate tube segment 202, where α has a value in the range of 30-70 °. The arrangement of the angle of the structure can effectively ensure that the catalyst c entering the cyclone chamber 101 from the catalyst feeding pipe 2 enters the cyclone chamber 101 along the direction tangential to the inner wall of the cyclone chamber 101 and attached to the inner wall of the cyclone chamber 101, and can perform spiral movement along the circumferential inner wall of the cyclone chamber 101 under the action of raw gas. Thereby further improving the contact efficiency of the raw material gas a after the catalyst c enters the cyclone chamber 101, improving the reaction efficiency, and simultaneously reducing the adjustment time required by the catalyst c for circumferential rotation along the inner wall of the cyclone chamber 101 after entering the cyclone chamber 101 from the catalyst feeding pipe 2 in the whole reaction process.
In an alternative embodiment of the utility model, the opening direction of the cambered surface opening 501 is away from the catalyst feed inlet 102 and the raw gas inlet 104 in the radial direction of the body 1, so that the catalyst c entering the cyclone chamber 101 from the catalyst feed inlet 102 enters the draft tube 5 through the cambered surface opening 501 under the action of inertia to influence the product gas b generated by the reaction in the cyclone reactor. Meanwhile, the raw material gas a entering the cyclone chamber 101 from the raw material gas inlet 104 is prevented from entering the drainage tube 5 under the inertia effect on the premise of no reaction, so that the production quality of the product gas b is influenced.
In a further alternative implementation of the present utility model, the number of the cambered surface openings 501 is plural, and the plurality of cambered surface openings 501 are arranged at intervals along the axial direction of the drainage tube 5, as shown in fig. 5, in a preferred embodiment of the present utility model, the opening lengths of the cambered surface openings 501 are both larger than the distances L3 and L4 between the adjacent cambered surface openings 501, and the design and the guarantee that the product gas b can enter into the drainage tube 5 through a sufficiently large opening area can also ensure the structural strength of the drainage tube 5, and ensure that the structure is not unstable due to the independent arrangement of the opening grooves during the operation, thereby generating the structural damage. In another further alternative embodiment of the present utility model, the opening size of the cambered surface opening 501 in the circumferential direction is θ, where the value of θ ranges from 40 ° to 60 °, and the angle setting of the opening size of the cambered surface opening 501 can avoid that the catalyst d enters the draft tube 5 from the cambered surface opening 501 due to the oversized opening during rotation, and can also avoid that the product gas b cannot enter the draft tube 5 quickly due to the oversized opening.
In a further alternative embodiment of the present utility model, when the cyclone reactor is placed horizontally, the catalyst feed pipe 2 is vertical to the horizontal direction, and the lower end face of the opening of the arc opening 501 is at an angle beta from the horizontal, preferably the value of beta is in the range of 5 deg. to 20 deg., so that the catalyst d and the product gas b can be effectively separated by the arrangement of the arc opening 501.
In an alternative embodiment of the present utility model, the product gas outlet 105 is connected with the product gas outlet pipe 6, the diameter of the drainage pipe 5 is larger than that of the product gas outlet pipe 6, the drainage pipe 5 is connected with the product gas outlet pipe 6 through the conical transition section 7, and the arrangement of the shrinkage opening from the drainage pipe 5 to the product gas outlet pipe 6, namely the arrangement of the conical transition section 7, can enable a pressure difference to be formed between the drainage pipe 5 and the product gas outlet pipe 6, so that the product gas b can be quickly and effectively led out of the drainage pipe 5.
In order to ensure that the draft tube 5 is sized to match the cyclone chamber 101 for better production testing, in an alternative embodiment of the present utility model, the cyclone reactor is sized such that the axial length L1 of the draft tube 5 is less than 4/5 of the axial length L0 of the cyclone chamber 101 to reserve a space for catalyst b to collect and rest for a catalyst outlet disposed at the rear end of the cyclone chamber 101. The size relation between the circumferential radius R2 of the draft tube 5 and the circumferential radius R1 of the cyclone chamber 101 is set to be 1/5R1 less than or equal to R2 less than or equal to 1/2R1, so that when the catalyst c and the raw material gas a perform spiral forward reaction along the inner wall of the cyclone chamber 101, the catalyst c cannot enter the draft tube 5 due to the fact that the interval between the inner wall of the cyclone chamber 101 and the inner wall of the draft tube 5 is too small, and meanwhile, the catalyst d and the product gas b cannot enter the draft tube 5 rapidly and effectively due to the fact that the interval between the inner wall of the cyclone chamber 101 and the inner wall of the draft tube 5 is too large after separation.
In an alternative embodiment of the utility model, the cyclone reactor further comprises a feed gas inlet distributor 4, which feed gas inlet distributor 4 is connected to the feed gas inlet 104 for dispersing feed gas into the cyclone chamber 101. The feed gas inlet distributor 4 includes a straight pipe 401 and a plurality of nozzles 402 communicating with the straight pipe 401, the plurality of nozzles 402 being arranged side by side in an inlet direction of the straight pipe 401 so as to split the feed gas a in the straight pipe 401. In a further alternative embodiment of the present utility model, the outlet end of the nozzle 402 is provided with a guide member 403 for guiding the raw material gas a in the nozzle 402 toward the direction of the catalyst discharge port 103 of the cyclone chamber 101, so that the reaction between the catalyst c and the raw material gas a can be better promoted, and the overall operation time can be shortened. In a further alternative embodiment of the present utility model, as shown in fig. 4, the guide member 403 is a tube with an inclined outlet end, and the axial direction of the outlet end of the guide member 403 and the axial direction of the nozzle 402 have an included angle γ, where γ has a value in the range of 0-60 °, and the arrangement of the inclined angle can effectively improve the pushing of the raw material gas a on the catalyst c, so as to realize the rotary flow of the catalyst c along the circumference of the inner wall, ensure the rapid and sufficient reaction, and avoid the long-time retention or the short-time end.
In an alternative embodiment of the present utility model, the catalyst discharge hole 103 is provided with a catalyst discharge groove 8 for blocking the flow of the catalyst d and gathering the catalyst, wherein the catalyst discharge hole 103 is arranged in the catalyst discharge groove 8, and the catalyst discharge groove 8 can hold the catalyst d, so that the catalyst d is prevented from gathering on the inner wall surface of the cyclone chamber 101, the ongoing reaction in the cyclone chamber 101 is affected, and meanwhile, the situation that the catalyst d directly flows out from the catalyst discharge hole 103 and easily causes the catalyst discharge hole 103 to be blocked is avoided.
In a further alternative embodiment of the present utility model, the catalyst discharging chute 8 has a funnel-shaped structure, the catalyst discharging port 103 is disposed in the middle of the catalyst discharging chute 8, and/or an included angle between a center line of the catalyst discharging port 103 and a vertical direction of an inlet direction of the raw material gas is phi, wherein the value of phi ranges from 0 ° to 45 °, and the arrangement of the structure and the angle ensures that the catalyst d is aggregated and is not easy to cause the catalyst discharging port 103 to be blocked due to the excessive flow out of the catalyst discharging port 103.
The second utility model provides a production method of low-carbon olefin, which adopts any one of the cyclone reactors, and the specific reaction flow of the production method is as follows:
a raw material gas a with the main component of methanol enters the cyclone chamber 101 from a raw material gas inlet 104, contacts with a catalyst c falling from a catalyst feeding pipe 2 in a near-wall cross-flow manner, reacts, and carries a catalyst d to flow around a central shaft along the peripheral wall of the cyclone chamber 101, at the moment, the raw material gas a reacts under the action of the catalyst c to form a product gas b, and the product gas b and the catalyst c jointly form a gas phase flow;
the gas phase flow carries the catalyst c and makes spiral flow around the center axis of the cyclone chamber 101 and along the direction of the catalyst discharge port 103 under the action of inertia and centrifugal force; in the spiral flow process, when the gas phase flow passes near the cambered surface opening 501 of the drainage tube 5, the catalyst c in the gas phase flow continuously rotates and flows along the inner wall surface under the inertia effect due to the higher density, the product gas b is separated from the solid phase catalyst c under the drainage effect, enters the drainage tube 5 through the cambered surface opening 501 and leaves the cyclone chamber 101 from the product gas outlet 105 to enter the downstream process flow;
as product gas b exits the vapor phase stream, catalyst c rapidly decays in inertial flow and eventually exits catalyst outlet 103 (i.e., catalyst d).
In an alternative embodiment of the present utility model, the method for producing low carbon olefins includes at least one of the following setup scenarios:
firstly, preheating a raw material gas a which enters the cyclone reactor and mainly contains methanol, wherein the preheating temperature is 100-200 ℃;
in a second scenario, the active component of the catalyst c entering the cyclone reactor is a SAPO-34 molecular sieve; preferably, the average carbon deposition of the catalyst c is 0.5-6wt%; further preferably, the carbon deposition of the catalyst c is 4wt% to 5wt%;
in the third scenario, the reaction temperature in the cyclone chamber 101 is 400-500 ℃ and the reaction pressure is 0.01-1 MPa.
In a further alternative embodiment of the present utility model, when the cyclone reactor includes the feed gas inlet distributor 4, the gas velocity of the feed gas a through the outlet nozzle 402 of the feed gas inlet distributor 4 is 10 to 30m/s;
the reaction contact time of the raw material gas a and the catalyst c in the cyclone chamber 101 is 0.1-2 s, preferably 0.2-0.5 s;
when the product gas outlet pipe 6 is connected to the product gas outlet 105, the product gas b exits the cyclone reactor through the product gas outlet pipe 6, and the flow velocity of the product gas b in the pipeline of the product gas outlet pipe 6 is 10-20 m/s.
The above description is only of the preferred embodiments of the present utility model and is not intended to limit the present utility model, but various modifications and variations can be made to the present utility model by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (16)
1. A cyclone reactor, the cyclone reactor comprising:
the cyclone reactor comprises a body (1), wherein the body (1) is a cylinder with two closed ends, a cyclone chamber (101) for carrying out gas material reaction is formed in the body (1), a catalyst feed port (102), a catalyst discharge port (103) and a raw gas inlet (104) are formed in the peripheral wall of the body (1), the catalyst feed port (102) and the catalyst discharge port (103) are respectively positioned at two axial ends of the body (1), the raw gas inlet (104) and the catalyst feed port (102) are positioned in the same circumferential direction of the body (1), and are arranged at the downstream of the feeding direction of the catalyst feed port (102), so that a catalyst entering the cyclone chamber (101) from the catalyst feed port (102) rotates to the catalyst discharge port (103) along the inner wall surface of the cyclone chamber (101) under the pushing of the raw gas, the raw gas is catalyzed to generate product gas, and the product gas is arranged on the end wall (105) of the body (1) close to the catalyst feed port (102); and
the cyclone separator comprises a drainage tube (5), wherein the drainage tube (5) is coaxially arranged in a cyclone chamber (101), one end of the drainage tube (5) is connected with a product gas outlet (105), and a cambered surface opening (501) for enabling product gas in the cyclone chamber (101) to enter the drainage tube (5) is formed in the tube wall of the drainage tube (5).
2. The cyclone reactor according to claim 1, characterized in that the cyclone reactor comprises a catalyst feed pipe (2) arranged at the catalyst feed inlet (102) for introducing catalyst into the cyclone chamber (101), the catalyst feed pipe (2) comprising a straight pipe section (201) arranged outside the cyclone chamber (101) and an arc pipe section (202) arranged against the inner wall surface of the cyclone chamber (101).
3. The cyclone reactor according to claim 2, characterized in that the angle between the centre line of the straight tube section (201) and the tangent of the curved tube section (202) is α, wherein α has a value in the range of 30-70 °.
4. Swirl reactor according to claim 1, characterised in that the opening direction of the cambered surface opening (501) is directed away from the catalyst feed opening (102) and the feed gas inlet (104) in the radial direction of the body (1).
5. The cyclone reactor according to claim 4, characterized in that the cambered surface opening (501) comprises at least one of the following:
in a first mode, a plurality of cambered surface openings (501) are formed, and the cambered surface openings (501) are arranged at intervals along the axial direction of the drainage tube (5);
in the second mode, the opening size of the cambered surface opening (501) in the circumferential direction is theta, wherein the value range of theta is 40-60 degrees.
6. The cyclone reactor according to claim 1, characterized in that a product gas outlet pipe (6) is connected at the product gas outlet (105), the diameter of the draft tube (5) is larger than the diameter of the product gas outlet pipe (6), and the draft tube (5) is connected with the product gas outlet pipe (6) through a conical transition section (7).
7. The cyclone reactor according to claim 1, characterized in that the axial length L1 of the draft tube (5) is less than 4/5 of the axial length L0 of the cyclone chamber (101); and/or the size relation between the radius R2 of the drainage tube (5) and the radius R1 of the cyclone chamber (101) is 1/5R 1-R2-1/2R 1.
8. The cyclone reactor according to claim 1, further comprising a feed gas inlet distributor (4), the feed gas inlet distributor (4) being connected to the feed gas inlet (104) for dispersing feed gas into the cyclone chamber (101).
9. The cyclone reactor according to claim 8, characterized in that the feed gas inlet distributor (4) comprises a straight-through pipe (401) and a plurality of nozzles (402) communicating with the straight-through pipe (401), the plurality of nozzles (402) being arranged side by side in an inlet direction perpendicular to the straight-through pipe (401) to split feed gas in the straight-through pipe (401).
10. The cyclone reactor according to claim 9, characterized in that the outlet end of the lance (402) is provided with a guide (403) for guiding the feed gas in the lance (402) in the direction of the catalyst discharge opening (103) of the cyclone chamber (101).
11. The cyclone reactor according to claim 10, wherein the guide (403) is a tube with an inclined outlet end, and the angle between the axial direction of the outlet end of the guide (403) and the axial direction of the nozzle (402) is γ, wherein γ has a value ranging from 0 ° to 60 °.
12. The cyclone reactor according to claim 1, characterized in that a catalyst discharge channel (8) for blocking the flow of catalyst and for collecting the catalyst is provided at the catalyst discharge opening (103), the catalyst discharge opening (103) being arranged in the catalyst discharge channel (8).
13. The cyclone reactor according to claim 12, characterized in that the catalyst discharge chute (8) is of a funnel-shaped structure, the catalyst discharge opening (103) being arranged in the middle of the catalyst discharge chute (8); and/or the included angle between the central line of the catalyst discharge port (103) and the vertical direction of the inlet direction of the raw material gas is phi, wherein the value range of phi is 0-45 degrees.
14. A process for the production of light olefins, characterized in that a cyclone reactor as claimed in any of the preceding claims 1 to 13 is used.
15. The method for producing light olefins according to claim 14, wherein the reaction conditions of the production method include at least one of the following conditions,
firstly, preheating raw material gas (a) which enters the cyclone reactor and mainly contains methanol, wherein the preheating temperature is 100-200 ℃;
scene two, wherein the active component of the catalyst (c) entering the cyclone reactor is SAPO-34 molecular sieve; preferably, the catalyst (c) has an average carbon deposition of 0.5wt% to 6wt%; further preferably, the catalyst (c) has an average carbon deposition of 4wt% to 5wt%;
and in a third scenario, the reaction temperature in the cyclone chamber (101) is 400-500 ℃ and the reaction pressure is 0.01-1 MPa.
16. The method for producing light olefins according to claim 14, wherein when the cyclone reactor comprises a feed gas inlet distributor (4), the gas velocity of the feed gas (a) through an outlet nozzle (402) of the feed gas inlet distributor (4) is 10 to 30m/s;
the reaction contact time of the raw material gas (a) and the catalyst (c) in the cyclone chamber (101) is 0.1-2 s, preferably the contact time is 0.2-0.5 s;
when the product gas outlet (105) is connected with the product gas outlet pipe (6), the product gas (b) is discharged from the cyclone reactor through the product gas outlet pipe (6), and the flow velocity of the product gas (b) in the pipeline of the product gas outlet pipe (6) is 10-20 m/s.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111243064.0A CN116020357A (en) | 2021-10-25 | 2021-10-25 | Cyclone reactor and method for producing low-carbon olefin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111243064.0A CN116020357A (en) | 2021-10-25 | 2021-10-25 | Cyclone reactor and method for producing low-carbon olefin |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116020357A true CN116020357A (en) | 2023-04-28 |
Family
ID=86076398
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111243064.0A Pending CN116020357A (en) | 2021-10-25 | 2021-10-25 | Cyclone reactor and method for producing low-carbon olefin |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116020357A (en) |
Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2004014538A1 (en) * | 2002-08-08 | 2004-02-19 | Uop Llc | Process and apparatus for the separation of the catalyst using a cyclone in a fcc process |
| US7601305B1 (en) * | 2006-02-02 | 2009-10-13 | Uop Llc | FCC swirl impeding separation apparatus |
| CN102533311A (en) * | 2010-12-30 | 2012-07-04 | 中国石油天然气集团公司 | Axial-flow ultrashort contact cyclone reactor |
| CN103409159A (en) * | 2013-09-05 | 2013-11-27 | 中国石油大学(华东) | Direct-current type short contact rotational flow reactor |
| CN103571518A (en) * | 2013-11-26 | 2014-02-12 | 袁培林 | Catalytic cracking processing technology of inferior oil |
| CN205288741U (en) * | 2015-12-09 | 2016-06-08 | 中国石油天然气集团公司 | A swirl jet for catalytic cracking unit |
| CN107583772A (en) * | 2016-07-07 | 2018-01-16 | 神华集团有限责任公司 | Multiphase cyclonic separation unit and cyclone separator |
| CN110467247A (en) * | 2019-08-20 | 2019-11-19 | 佛山市中顺水处理科技有限公司 | Machine power Cyclonic reactor and reaction cell system |
| CN111054277A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Reactor and method for producing low-carbon olefin |
| CN111054276A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Reactor and process for producing olefin by converting methanol |
| CN112237896A (en) * | 2020-09-21 | 2021-01-19 | 中国石油大学(华东) | Novel mixing-enhanced reactor for alkylation of ionic liquid |
| CN112705127A (en) * | 2019-10-24 | 2021-04-27 | 中国石油化工股份有限公司 | Reactor and method for producing low-carbon olefin |
| CN113398847A (en) * | 2021-06-04 | 2021-09-17 | 中国石油大学(华东) | Intensive mixed cyclone reactor for ionic liquid alkylation |
-
2021
- 2021-10-25 CN CN202111243064.0A patent/CN116020357A/en active Pending
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2004014538A1 (en) * | 2002-08-08 | 2004-02-19 | Uop Llc | Process and apparatus for the separation of the catalyst using a cyclone in a fcc process |
| US7601305B1 (en) * | 2006-02-02 | 2009-10-13 | Uop Llc | FCC swirl impeding separation apparatus |
| CN102533311A (en) * | 2010-12-30 | 2012-07-04 | 中国石油天然气集团公司 | Axial-flow ultrashort contact cyclone reactor |
| CN103409159A (en) * | 2013-09-05 | 2013-11-27 | 中国石油大学(华东) | Direct-current type short contact rotational flow reactor |
| CN103571518A (en) * | 2013-11-26 | 2014-02-12 | 袁培林 | Catalytic cracking processing technology of inferior oil |
| CN205288741U (en) * | 2015-12-09 | 2016-06-08 | 中国石油天然气集团公司 | A swirl jet for catalytic cracking unit |
| CN107583772A (en) * | 2016-07-07 | 2018-01-16 | 神华集团有限责任公司 | Multiphase cyclonic separation unit and cyclone separator |
| CN111054277A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Reactor and method for producing low-carbon olefin |
| CN111054276A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Reactor and process for producing olefin by converting methanol |
| CN110467247A (en) * | 2019-08-20 | 2019-11-19 | 佛山市中顺水处理科技有限公司 | Machine power Cyclonic reactor and reaction cell system |
| CN112705127A (en) * | 2019-10-24 | 2021-04-27 | 中国石油化工股份有限公司 | Reactor and method for producing low-carbon olefin |
| CN112237896A (en) * | 2020-09-21 | 2021-01-19 | 中国石油大学(华东) | Novel mixing-enhanced reactor for alkylation of ionic liquid |
| CN113398847A (en) * | 2021-06-04 | 2021-09-17 | 中国石油大学(华东) | Intensive mixed cyclone reactor for ionic liquid alkylation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| TWI661867B (en) | Fluidized bed reactor, reaction regeneration equipment, method for preparing olefin, and method for preparing aromatic hydrocarbon | |
| RU2002108352A (en) | INITIAL MATERIAL INJECTION SYSTEM FOR CATALYTIC CRACKING PROCESS | |
| CN109012513A (en) | A kind of methanol to olefins reaction device | |
| CN113663607A (en) | Downer reactor and method of operating same | |
| CN110449112A (en) | A kind of pseudocumene continuous oxidation reaction device | |
| CN116020357A (en) | Cyclone reactor and method for producing low-carbon olefin | |
| CN111054277B (en) | Reactor and method for producing low-carbon olefin | |
| CN101524610A (en) | Vortex flow quick separation equipment at outlet of high-efficiency riser with conical flow isolating cylinder | |
| CN112705127B (en) | Reactor and method for producing low-carbon olefin | |
| CN111054276A (en) | Reactor and process for producing olefin by converting methanol | |
| US20110198267A1 (en) | Advanced elevated feed distribution apparatus and process for large diameter fcc reactor risers | |
| CN112708447B (en) | Riser reactor capable of reducing back mixing of side wall area | |
| CN215196858U (en) | Novel distributor of acrylonitrile device reactor | |
| EP3854772B1 (en) | Method for catalytic cracking of naphtha | |
| CN210787366U (en) | Continuous oxidation reactor for unsym-trimethyl benzene | |
| CN102397725B (en) | Horizontal type gas-solid ultra-short rapid separation apparatus with nonuniform slits on gas exhaust pipe | |
| CN115501822B (en) | Convection type fluidized bed reactor and application thereof | |
| CN112246192A (en) | Petrochemical fluidized bed reactor and application thereof | |
| CN115501822A (en) | Convection type fluidized bed reactor and application thereof | |
| CN117920058A (en) | Spiral casing reactor, reaction system, application of spiral casing reactor and method for producing low-carbon olefin | |
| CN114425248B (en) | Catalytic converter mixer, device for producing low-carbon olefin and method and application for producing low-carbon olefin | |
| CN212549474U (en) | Conical distribution plate of gas phase reactor | |
| CN216864088U (en) | Clean fuel production riser reactor | |
| CN115501823B (en) | Fluidized bed reactor, device for preparing low-carbon olefin and method for preparing low-carbon olefin | |
| CN111715153B (en) | Alkane dehydrogenation circulating fluidized bed reaction device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |