WO2020190175A2 - Répartiteurs de catalyseur et de gaz de transport pour systèmes de circulation de réacteur-régénérateur à lit fluidisé - Google Patents

Répartiteurs de catalyseur et de gaz de transport pour systèmes de circulation de réacteur-régénérateur à lit fluidisé Download PDF

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Publication number
WO2020190175A2
WO2020190175A2 PCT/RU2020/000147 RU2020000147W WO2020190175A2 WO 2020190175 A2 WO2020190175 A2 WO 2020190175A2 RU 2020000147 W RU2020000147 W RU 2020000147W WO 2020190175 A2 WO2020190175 A2 WO 2020190175A2
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WO
WIPO (PCT)
Prior art keywords
disc
distributor according
catalyst
transport pipe
reactor
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.)
Ceased
Application number
PCT/RU2020/000147
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English (en)
Russian (ru)
Other versions
WO2020190175A3 (fr
Inventor
Станислав Михайлович КОМАРОВ
Александра Станиславовна ХАРЧЕНКО
Алексей Александрович КРЕЙКЕР
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Special Design and Engineering Bureau Katalizator JSC
Original Assignee
Special Design and Engineering Bureau Katalizator JSC
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Special Design and Engineering Bureau Katalizator JSC filed Critical Special Design and Engineering Bureau Katalizator JSC
Publication of WO2020190175A2 publication Critical patent/WO2020190175A2/fr
Publication of WO2020190175A3 publication Critical patent/WO2020190175A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
    • C07C5/333—Catalytic processes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Definitions

  • the invention relates to the field of petrochemistry, in particular to installations for the dehydrogenation of paraffinic hydrocarbons C3-C5 into the corresponding olefinic hydrocarbons used to obtain basic monomers for synthetic rubber, as well as in the production of polypropylene, methyl tertiary butyl ether, etc.
  • These devices are located in the upper part of the reactor and / or regenerator in the separation zone above the fluidized bed level and include a baffle disk of a conical or elliptical shape located above the upper end of a transport pipe with an upward flow of a mixture of catalyst and transport gas.
  • the disadvantages of the known catalyst distributor include the possibility of the capture of catalyst particles by the gas flow of the reactor and / or the regenerator at the outlet of the distributor, which leads to an increase in the carryover (losses) of the catalyst from the reactor-regenerator system.
  • the transport gas in the variants of feeding the catalyst to the reactor for the feedstock vapor and air - in the regenerator does not contact with the fluidized bed, respectively, in the reactor and regenerator, mixing with the contact gas and the regeneration gas in the separation zones of these devices.
  • the value of these flows reaches 5% or more of the amount of raw material supplied to the reactor or air to the regenerator.
  • Unreacted paraffinic hydrocarbons from the transport gas ballast the contact gas go through the entire technological cycle and return with recycling unreacted paraffinic hydrocarbons of the feedstock at the entrance to the reactor, which leads to corresponding energy costs and losses of a part of the said paraffinic hydrocarbons of the transport gas in production.
  • oxygen in the air supplied to transport the catalyst to the regenerator is not used for catalyst regeneration, for example, for burning off coke in the regenerator.
  • the disadvantage of this distributor also includes the presence of significant thermal irregularities in the upper part of the fluidized bed of the reactor and the regenerator due to the uneven distribution of the catalyst over the cross section of the fluidized bed, which reduces the yields of olefinic hydrocarbons.
  • the reactor and / or regenerator contains a vertical transport pipe located along their axis of the reactor and / or the regenerator with an ascending flow of a mixture of catalyst and transport gas, connected to an expander installed coaxially with the pipe at its upper end, containing a cylindrical shell, a bottom and cover.
  • the expander is equipped with connecting pipes with vertical risers with a descending flow of the mixture of catalyst and transport gas, the lower ends of which are located under the level of the fluidized bed of the catalyst above the upper sectioning grid.
  • the distributor contains a vertical transport pipe located along the axis of the regenerator with an ascending flow of catalyst and transport gas, installed with an open end upward, an expander located coaxially with it, containing a bottom connected to the end of the transport pipe and made in the form of a first disk surrounding the opening of the pipe end, and a cover in the form of a second disk with the latter located at some distance upward from the first disk with the formation of an annular gap between the disks, open for the outflow of catalyst and transport gas.
  • the objective of the present invention is to reduce the erosion of the distributor elements, to increase the yields of olefinic hydrocarbons for the passed and decomposed feedstock, to reduce the air consumption for catalyst regeneration, and to reduce catalyst carryover.
  • a catalyst and transport gas distributor for circulation systems is proposed: a C 3 -C 5 paraffinic hydrocarbon dehydrogenation reactor-regenerator with sectioned fluidized bed gratings containing a supply transport pipe 19 connected to a vertical transport pipe 1 located along the axis of the reactor and / or regenerator with an upward or downward flow of catalyst and transport gas, installed open end 2, respectively up or down, an expander located coaxially with it, containing a bottom connected to the end 2 of the transport pipe 1, and a cover in which the bottom of the expander consists of a diffuser 6 in the form of a truncated a cone connected by a smaller base with an open end 2 by a transport pipe 1, and a large base 7 with a first disc 8 surrounding the diffuser opening 6, and the cover includes a bottom and a second disc 12, while the second disc 12 is connected to the end of the bottom, surrounding it, is installed at a certain distance up or down from the first disc 8 rigidly to form an open annular space 20 between the
  • the cover may contain an elliptical 10, or a spherical 11, or a conical 16 bottom.
  • the expander cover may additionally include a cylindrical shell 13 connected to the end mounted on its upper 14 or lower 15
  • the diameter of the end of the bottom or the lower opening of the shell 13 can be greater than the diameter of the larger opening of the diffuser 6, while the edges of the end of the bottom or the opening of the shell 13 can lie on the generatrix of the cone of the diffuser 6.
  • a reflective cone 17 can be attached to the bottom of the lid with its base, which can be directed upward or downward and installed centrally above or below the open end 2 of the transport pipe 1.
  • the ratio of the diameter of the base of the reflective cone 17 to the diameter of the larger base 7 of the diffuser 6 can be in the range from 0.30 to 1.20.
  • the first disc 8 can be installed horizontally.
  • the first disc 8 can have the shape of a frusto-cone and be installed with an inclination of the generatrix of the cone at an angle ranging from 30 ° upward from the horizontal position and up to 30 ° downward.
  • the second disc 12 can be installed horizontally.
  • the second disc 12 may have the shape of a frusto-cone and be installed with an inclination of the generatrix of the cone at an angle ranging from 30 ° upward from the horizontal position and up to 45 ° downward.
  • the second disc 12 is at the same time the bottom and has the shape of a cone or truncated cone.
  • the second disc 12 can be installed with an inclination of the generatrix of the cone at an angle ranging from 30 ° upward from the horizontal position and up to 45 ° downward.
  • the ratio of the diameter of the first disc 8 to the diameter of the reactor or regenerator can range from 0.10 to 0.50.
  • the ratio of the diameter of the first disc 8 to the diameter of the second disc 12 can range from 0.80 to 1.25.
  • the second disc 12 can be rigidly connected to the first disc 8 by means of partitions 21.
  • the number of baffles 21 can range from 3.00 to 8.00.
  • Baffles 21 can be evenly spaced around the circumference of the discs, dividing the open annular space 20 into sections.
  • the baffles 21 can be flat radially directed plates.
  • the inserts can be installed at an angle to the radial direction in the range of values from 3 ° to 45 °.
  • the plates can be bent in a spiral shape.
  • the expander can be located above or below the level of the fluidized bed above the upper sectioning grid.
  • the supply transport pipe 19 can be removed from the fluidized bed of the reactor and / or the regenerator in whole or in part and be located outside the said apparatus for design reasons or in connection with technological limitations.
  • the supply transport pipe 19 with the catalyst superheated in the regenerator directed to the reactor should be removed from the desorption cup of the circulating catalyst in the lower part of the reactor or from the desorption cup and the fluidized bed of the dehydrogenation zone of the reactor in order to avoid the formation of coke on the "hot" surface of the supply transport pipes 19.
  • the supply transport pipe 19 is connected to the transport pipe 1 of the distributor through the use of a connecting transport pipe 5 and swivel elbows 3 and 4.
  • the technical result is that the proposed design of the distributor of the transport gas and the catalyst circulating in the system reactor-regenerator for dehydrogenation of paraffinic hydrocarbons C 3 -C 5 with a fluidized bed, in comparison with the known design, reduces the erosion of the structural elements of the distributor and internal devices of the reactor and the regenerator, increases the outputs olefinic hydrocarbons, reduced air consumption for catalyst regeneration, reduced catalyst carryover.
  • Figures 1-4 show some possible variants of catalyst and transport gas distributors for circulation systems of a C 3 -C 5 paraffinic hydrocarbon dehydrogenation regenerator with sectioned fluidized bed gratings in accordance with the present invention.
  • the distributor comprises a vertical transport pipe 1 located along the axis of the reactor and / or the regenerator with an ascending (FIGS. 1 and 2) flow 9 of catalyst and transport gas, installed with its open end 2 upward.
  • the distributor contains a vertical transport pipe 1 located along the axis of the reactor and / or the regenerator with a descending (Fig. 3 and 4) flow 18 of catalyst and transport gas, installed with the open end 2 down and with the help of rotary bends 3 and 4 with the end 2 down ...
  • the descending flow is organized, for example, in connection with the possible location of the supply transport pipe 19 not along the axis of the reactor or regenerator (Fig. 3) or the location of the supply transport pipe 19 outside the reactor or regenerator (Fig. 4).
  • the distributors also contain an expander located coaxially with the vertical transport pipe 1, containing a cover and a bottom, consisting of a diffuser 6 in the form of a truncated cone connected by a smaller base with end 2 (Figs. 1 and 2) and end 2 (Figs. 3 and 4) of the transport pipes 1, and a large base 7 with the first disc 8 surrounding the diffuser opening 6.
  • Cover the expander consists of an elliptical 10 (Fig. 3) or spherical And (Fig. 1) or conical 16 (Fig. 2) bottom and a second disc 12 (Fig. 3) installed at the end of the bottom, surrounding it, while the second disc 12 installed at a certain distance upward (Fig. 1 and 2) or down (Fig. 3 and 4) from the first disc 8 to form an open annular space 20 between the discs.
  • the cover (Fig. 1) consists of a cylindrical shell 13, connected to a spherical bottom 11 mounted on its upper end 14 and, accordingly, at its lower end 15 by a second disc 12 surrounding the shell hole 13.
  • the diameter of the end of the elliptical bottom 10 (Fig. 3) or the lower opening of the shell 13 (Fig. 1) is greater than the diameter of the larger opening of the diffuser 6, while the edges of the end of the elliptical bottom 10 or the opening of the shell 13 lie on the generatrix of the cone of the diffuser 6.
  • a reflective cone 17 is attached to the bottom with its base, and the reflective cone can be directed downward (Fig. 2) or upward (Fig. 4) and installed centrally above or below the open end 2 of the transport pipe 1.
  • the ratio of the diameter of the base of the reflective cone 17 to the diameter of the transport pipe 1 can be in the range from 0.30 to 1.50.
  • the first disc 8 (Fig. 1, 2) is installed horizontally.
  • the first disc 8 (FIGS. 3, 4) has a frusto-conical shape.
  • the second disc 12 (Fig. 3) is installed horizontally.
  • the second disc 12 has a frusto-conical shape (Fig. 1).
  • the second disc 12 is at the same time the bottom and has the shape of a cone (Fig. 2) or a truncated cone (Fig. 4).
  • the second disc 12 is rigidly connected to the first disc 8 by means of partitions 21 (Figs. 5-7).
  • the baffles 21 are evenly spaced around the circumference of the discs, dividing the open annular space 20 into sections.
  • the baffles 21 are flat radially directed plates (FIG. 5).
  • the partitions 21 are installed at an angle to the radial direction (Fig. 6).
  • the baffles 21 are bent in a spiral shape (Fig. 7).
  • various types of spirals can be used, such as Archimedean, hyperbolic, logarithmic, etc. Preferred is the sweep (involute) of the circumference of the larger base 7 of the cone of the diffuser 6.
  • the expander is located above (Fig. 3) or below (Fig. 4) the level of the fluidized bed above the upper sectioning grid.
  • the proposed distributor works as follows.
  • a system of pneumatic transport of the catalyst is used with a preferred linear velocity of the gas flow in vertically installed transport pipes in the range from 4 m / s to 12 m / s ...
  • vapors of raw materials when transporting a catalyst to a reactor
  • air when transporting a catalyst to a regenerator
  • the mixture of the circulating catalyst and transport gas enters the reactor or regenerator in an upward flow (FIGS. 1, 2) or a downflow (FIG. 3, 4) through a transport pipe 1. Then the mixture of catalyst and transport gas passes through a diffuser 6, with an angle diffuser opening a equal to 10 ° -60 °.
  • a regime is realized that approaches the continuous flow of the gas flow along the diffuser 6, and practically excludes the phenomena of reverse circulation of gas and catalyst with strongly pulsating separated flows in the zone adjacent to the first disk 8, excluding the erosion of the latter. Reducing the opening angle of the diffuser 6 to values less than 10 ° becomes unacceptable due to design restrictions along the length of the diffuser 6.
  • the velocity of the transport gas and catalyst decreases, the concentration irregularities in the flow decrease, and the hydraulic resistance at the entrance to the open annular space decreases 20.
  • the gas flow, leaving the diffuser 6, is uniformly diverted into the open annular space 20, and the catalyst flow by inertia reaches the surface of the bottoms 11 and 10 (Figs. 1 and 3) or the conical bottom 16 s reflective cone 17 (figure 2 and 4) at significantly lower speeds than in the prototype.
  • a suspended layer of a constantly exchanging catalyst accumulates, which, together with a decrease in flow rates, sharply reduces the erosion of the surfaces of these structural elements.
  • the catalyst enters the volume of the bottoms, mainly in their central part, is retained in the suspended bed, where the irregularities of the catalyst flow are averaged, and flows out through the peripheral part of the bottoms. If the conditions claimed in the invention are met - "the diameter of the end of the bottom 10 (Fig. 3) or the lower opening of the shell 13 (Fig.
  • the catalyst is delayed in the initial section of the annular space 20 and then, under the influence of the transport gas flow, a significant increase in the catalyst flow rate in the final section of the said space occurs.
  • This situation is ensured by the claimed range of sizes of the structural elements of the distributor.
  • Increasing the flow rate of the mixture of catalyst and transport gas allows the catalyst and gas to be discharged from the annular slot of the distributor at a significant distance from the outer edge of the discs.
  • the transport gas is dispersed in the distributor and at the point of entry into the fluidized bed is in a state of fine bubbles.
  • the high flow rate of the catalyst and transport gas in the radial direction improves the mixing of the catalyst and transport gas in the fluidized bed.
  • the first discs are shown mounted horizontally, they can also be mounted in the form of cones with a preferred downward inclination of the generatrix of the cones (Fig. 3, 4).
  • the conical shape of the disks (Figs. 1-4) with a downward slope of the generatrix of the cones prevents the accumulation of catalyst on the surfaces of these disks and, accordingly, when using the distributor in the reactor, prevents the deposition of monolithic coke on these structural elements, which increases the stability of the distributor and the reactor as a whole ...
  • the specified space When sectioning an open annular space with partitions, the specified space is divided into independent channels, which ensures the preservation of the uniformity of the distribution of flows when they flow out along the channels.
  • the diameter of the reactor is 5.1 m.
  • the diameter of the regenerator is 5.1 m.
  • the diameter of the transport pipe of the reactor-regenerator is 300 mm.
  • the diameter of the regenerator-reactor transport pipe is 300 mm.
  • the proposed distributors can be used in the field of petrochemistry, in installations for the dehydrogenation of C3-C5 paraffinic hydrocarbons into the corresponding olefinic hydrocarbons used to obtain basic monomers for synthetic rubber, as well as in the production of polypropylene, methyl tertiary butyl ether, etc.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention se rapporte au domaine de la pétrochimie et concerne notamment des installations de déshydrogénation d'hydrocarbures paraffiniques С3-С5 en hydrocarbures oléfiniques correspondants. L'invention concerne un répartiteur de catalyseur et de gaz de transport pour des systèmes de circulation de réacteur-régénérateur de déshydrogénation d'hydrocarbures paraffiniques С3-С5 avec des grilles sectionnées par un lit fluidisé, lequel comprend un tube de transport (19) connecté à un tube de transport vertical (1) disposé le long de l'axe du réacteur et/ou régénérateur, comprenant un flux ascendant ou descendant de catalyseur et de gaz de transport, et disposé avec l'extrémité ouverte (2) vers le haut ou vers le bas, respectivement; il comprend également un détendeur disposé coaxialement à celui-ci et comprenant un fond connecté à l'extrémité (2) du tube de transport (1), et un couvercle. Le fond du détendeur se compose d'un diffuseur (6) en forme de cône tronqué connecté par la petite base à l'extrémité ouverte (2) du tube de transport (1) et, par par la grande base (7), à un premier disque (8) entourant l'ouverture du diffuseur (6); le couvercle comprend un fond et un second disque (12); le second disque (12) est connecté à l'extrémité du fond et, en l'entourant, est disposé à une certaine distance en dessus ou en dessous du premier disque (8) de manière rigide afin de former entre les disques un espace annulaire ouvert (20); l'angle du diffuseur (6) varie de 10° à 60°. Le résultat technique consiste en une érosion moindre des éléments de la structure du répartiteur et des dispositifs internes du réacteur et du régénérateur, en une augmentation de la production d'hydrocarbures oléfiniques, en une diminution de la consommation d'air pour la régénération du catalyseur, et en une diminution de l'usure du catalyseur.
PCT/RU2020/000147 2019-03-20 2020-03-19 Répartiteurs de catalyseur et de gaz de transport pour systèmes de circulation de réacteur-régénérateur à lit fluidisé Ceased WO2020190175A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU2019107956 2019-03-20
RU2019107956A RU2694840C1 (ru) 2019-03-20 2019-03-20 Распределители катализатора и транспортного газа для систем циркуляции реактор-регенератор с кипящим слоем

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WO2020190175A2 true WO2020190175A2 (fr) 2020-09-24
WO2020190175A3 WO2020190175A3 (fr) 2020-11-26

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115301075A (zh) * 2022-09-01 2022-11-08 四川能投建工集团设计研究院有限公司 一种硫磺制酸尾气处理装置

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2767249C1 (ru) * 2021-04-09 2022-03-17 Открытое акционерное общество "Научно-исследовательский институт "Ярсинтез" (ОАО НИИ "Ярсинтез") Распределитель катализатора и транспортного газа

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2611685A (en) * 1950-11-22 1952-09-23 Standard Oil Dev Co Fluid distributor for vessels
US6797239B1 (en) * 2000-11-22 2004-09-28 Shell Oil Company Spent catalyst distributor
RU2652198C1 (ru) * 2017-07-04 2018-04-25 Акционерное общество "Специальное конструкторско-технологическое бюро "Катализатор" Распределитель катализатора для системы реактор-регенератор дегидрирования парафиновых углеводородов С3-С5 с кипящим слоем
RU2652195C1 (ru) * 2017-07-04 2018-04-25 Акционерное общество "Специальное конструкторско-технологическое бюро "Катализатор" Распределитель катализатора и транспортного газа для системы реактор - регенератор дегидрирования парафиновых углеводородов С3-С5 с кипящим слоем

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115301075A (zh) * 2022-09-01 2022-11-08 四川能投建工集团设计研究院有限公司 一种硫磺制酸尾气处理装置
CN115301075B (zh) * 2022-09-01 2024-03-19 四川能投建工集团设计研究院有限公司 一种硫磺制酸尾气处理装置

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RU2694840C1 (ru) 2019-07-17

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