• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The invention relates to catalytic conversion of fluid introduced into the upper end of a vessel (1), passed through a catalyst bed in the vessel (1), passed through passages (20) between guide elements (14) arranged in the vessel (1), and removed from the lower end of the vessel (1), wherein at or near the narrow parts of the passages (20) cooling fluid is introduced into the passages (20) to control the temperature in the catalyst bed.
    公开号:SU1523047A3
    申请号:SU864027658
    申请日:1986-06-16
    公开日:1989-11-15
    发明作者:Уильям Белл Вестерман Дэвид；Мишель Скотт Эндрю
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий, Б.В. (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to devices for carrying out a process for the catalytic conversion of a liquid and / or gas and can be used to produce a synthesis gas consisting of hydrogen and carbon monoxide.
    The purpose of the invention is to intensify the process by uniformly distributing the liquid and the catalyst.
    FIG. 1 is a schematic representation of a device, a vertical section j .. in FIG. 2 - section A-A in FIG. 1; in fig. 3 shows the node I in FIG. one; in fig. 4 shows a modified version of the design of the guide element, a slit.
    The catalytic conversion apparatus includes a reactor 1, an inlet 2 for the liquid and an inlet 3 for the catalyst located at the upper end of the reactor I5 and an exhaust nozzle .4 for the liquid and an outlet for the catalyst 5 located at the lower end of the reactor 1. Inside the reactor 1 there is a support body 6 supporting a bed of catalyst particles (not shown) with a central hole 7 which is connected to the outflow pipe 5 for the catalyst by pipe 8. The latter is equipped with a valve (not shown) allowing at the right time to unload the reactor 1 from the powdered catalyst.
    Inside reactor 1, first 9 and second 10 lattices are mounted at different levels, the planes of which are oriented perpendicular to the direction of the O1 tsD
    WITH

    S
    The flow of fluid in the reactor 1. Each lattice 9 and 10 is formed by a set of guide elements that are connected to the ends with an annular support element 11 mounted on the inner surface of the side wall of the reactor 1. The guide elements of the first lattice 9 are placed in a staggered manner. elements of the second lattice 10.
    Between the parts of the outer surfaces of adjacent guideways 12 elements facing one another and between the parts facing one another of the ankle surfaces of the annular support element I and the adjacent guide elements, channels 13 are formed. Each channel 13 in the direction of fluid flow has a narrowing 14, a narrow 15 and an expanding 16 part.
    Each guide element 12 has a triangular fluid tube 17 consisting of side walls 18 and a bottom wall 19 defining a fluid passage channel 20. Each annular support element J1 also includes a triangle tube 21 having a side wall 18 and the BOTTOM wall 19, limiting the fluid channels 22, connected to the channels 20, formed three-sided tubes 17 and to the inlet 23 for supplying the auxiliary liquid to the reactor.
    Triangular tubes 17 and 21 are mounted on support beams 24. The width of the bottom wall 19 of each triangular tube 17 and 21 is slightly greater than the width of the support beam 24, so that the edges of the bottom wall 19 protrude beyond the support beam 24 along its entire length. The protruding edges of the bottom wall 19 of each trihedral tube 17 and tube 21 protrude beyond the support section. Through holes 25 are made through some of the channels 20 and 22 of the pipes 17 and 21, respectively, the liquid from these pipes is fed into the channels 13 between adjacent guide elements. 12.
     The design of the guide elements and the annular support element of the second grid 10 is no different from the corresponding elements of the described first grid 9.
    The device for the process of catalytic conversion of sulfur-containing mineral oil into sulfur-free mineral oil using hydrogen works as follows.
    Initially, the powder catalyst is introduced into reactor 1 through inlet 3. This process continues until the reactor volume above support cone 6 and pipe B are filled with catalyst particles (not shown).
    After loading the reactor 1 with a catalyst, a mixture of sulfur-containing mineral oil and hydrogen is fed into it through an inlet pipe 2 under pressure within 3 to 25 Sha,
    heated to a temperature in the range of 300 - 500 ° C.
    In the process of exothermic reaction. Hydrogen sulfide is formed between hydrogen and sulfur contained in mineral oil, and the sulfur content of the original mineral oil is reduced to a minimum. The mixture of mineral oil and hydrogen sulfide in the reactor i moves to the downward and through the holes 26 in the wall of the pipe 8 enters the receiver 2.7 below the reference cone 6, from where it is removed through the spout 4. When cooled in an appropriate separator (not shown) formed during After the catalyst reaches a certain degree of poisoning, for example, after 6–12 months, the conversion process is stopped, the entire spent catalyst is removed from the reactor 1 reactor filled with fresh or regenerated catalyst.
    The temperature control in the reactor during the conversion process is carried out by supplying the coolant to the reactor, which can
    cooled desulfated mineral oil or a cooling gas should be used. The flow of coolant or gas into the reactor is pro- duced through the inlet 23,
    connecting at least one of the grids 9 and 10, the cooling liquid enters the channels 13 between the guide elements 2 through from. 515
    versti 25 near narrow parts 15 channels 20,
    Thus, the cooling of the reaction products occurs in narrow parts of the passages j where the velocity of the fluid is at its maximum and where an increased flow ratio of the fluid flow is observed, thereby improving the heat exchange between the hot reaction products and the coolant.
    In order to achieve sufficiently intensive heat exchange with a moderate pressure drop across the grid, the total area of the channels 13 between the guide elements 12 should be within 30–60% of the cross sectional area of the reactor 1, preferably within 45–55%.
    The edges of the lower walls 19 triangular tubes 17 and 21 are released over the upper edges of the support beams. When the reactor powder 1 is loaded with catalyst powder (not shown), the mass of catalyst particles is distributed inside the reactor in such a way that under the edges of the lower walls 19 of the tubes 17 and 21 protruding beyond the edges of the support beams 24, the spaces 28 of the catalyst particles are unfilled over the entire length of the support beams 24. Since the openings 25 are located on the protruding beyond the edges of the supporting beams 24, the edges of the lower walls 19 of the tubes 17 and 21, the coolant flowing from these openings into the unfilled catalyst spaces 28, its penetration into the catalyst bed is distributed sporadically along the entire length of the support beams 24. Such a uniform distribution of cooling fluid along the length of the guide elements 12 ensures that a more uniform temperature distribution in the catalyst bed in the zone of the channels 13 is achieved.
    In order to evenly distribute the liquid in the expansion part 16 of each channel 13, the magnitude of the strictly angle 29 between the outer surface of the guide element 12 or the annular support element 11 and the vertical straight line must be matched with the value of the angle of divergence of the liquid. For liquids passing through a layer of ordinary powdered
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    catalyst, the acute angle 29 can be within 3 - JO.
    The even distribution of the liquid in the expansion part 16 of each channel 13 has a positive effect on the efficiency of the reaction, since in the case of uneven contact of the liquid with the catalyst, the temperature distribution in the catalyst bed is uneven - Hbif-i, and this causes uneven poisoning of the catalyst.
    The design of the converter described above makes it possible to use the catalyst without regenerating it for very long periods. When converters of the proposed design are used, the replacement of the catalyst can be performed not completely, but in parts, for which after a certain period of time it is necessary to remove a certain part of the catalyst from the reactor and replenish the reactor with a lean amount of fresh catalyst through the inlet 3. the catalyst loading process with the catalyst being simultaneously removed from the reactor, a complete catalyst change in the reactor can be carried out during rcoh period of time, for example within one day.
    In order for the downward movement of the catalyst particles in the converging part 14 of the channel 13 to be uniform, i.e. In order for the catalyst particles near the surfaces of the guide elements in the tapered part 14 of the channel 13 and in the central zone of the tapered part 14 to move at the same speed, the acute angle 30 between the vertical straight and the outer surface of the guide element 12 or the annular support element 11 B The narrowing part 14 of the channel 13 should be chosen in such a way that it ensures that fluidized particles are received in this passage. When conventional powdered catalysts are used in the converter in question, the magnitude of this acute angle 30 may be in the range of 10-40 °.
    The reactor may be used to carry out the conversion.
    these gases are in gas storage. In this case, the initial mixture of gas and liquid is injected into the reactor through the inlet 2,
    An example of such a conversion process is the conversion process of synthesis gas containing hydrogen and carbon monoxide into a liquid hydrocarbon.
    with those of boiling temperature in the range of boiling temperatures of middle distilled;
    l tov,
    In this process of conversion, the mixture of synthesis gas and returned in the process of recycled liquid hydrocarbon is heated to a temperature in the range of 200 - 250 ° C under pressure
    In the range of 2-4 MPa, a catalyst bed is introduced into the reactor. In this process, the liquid serves as a coolant, ensuring uniform temperature distribution in the bed of catalyst found in the reactor. During normal operation of the reactor, the surrounding hydrocarbon product is fed into the reactor through inlet 13, from where it enters the catalyst bed through pipes 17 and 21 and through openings 25, providing cooling of the reaction products inside the converter.
    The described reactor 1 (Fig. 0) has two lattices of guide elements. Reactors of small volume can have only one grid of guide elements. In large reactors, several lattices of guide elements can be used, for example 3 - 10, located inside the reactor at different levels. x
    In the guide elements, the holes for introducing coolant into the passages between adjacent elements are located along the edges of the bottom wall 19 of the trihedral tube 17 protruding behind the support beam 24, so that during normal operation of the converter, the cooling fluid is introduced narrow part 15 of channel 13.
    In accordance with the invention, a part of the guiding elements i2 in the grids 9 and 10, or all of these elements can be replaced by the guiding elements 31. The design of the latter includes a triangular tube 32 mounted on the supporting
    eight
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    the beam 33.-Kamada side wall of the triangular 32 consists of it 34 and the top 35 strips extending along the entire length of the guide element 31. The bottom 34 and top 35 strips forming the side wall of the triangular tube 32 are placed one relative to the other in such a way that the lower edge of the upper strip 35 is offset from the upper edge of the lower strip 34. Additional cooling fluid is introduced into the narrowing part of the passage between adjacent guide elements through a series of holes 36 located in that part of the side wall of the triangular pipe. killers 32, where the lower edge of the upper band 35 protrudes. at the upper edge of the lower strip 34, and extending along the entire length of the guide element.
    The lower CTaiiKa 37 of the triangular tube 32 protrudes in both directions beyond the edges of the support beam 33. In these protruding edges of the bottom wall 34 of the triangular tube 32, holes 38 are made to supply additional lashiness. a passage between adjacent guide elements 31 and uniformly distributed along the entire length of the guide element.
    The holes 36 and 38 connect the inner channel 39 of the triangular tube 32 to the space between the adjacent guide elements 31 in its narrowing and narrowest parts, respectively. The channel 39 of the triangular tube 32 is connected to the channel 22 of the annular support element 11,
    During normal operation of the reactor, the catalyst-filled powder (non-shown) filling the internal volume of the reactor is distributed in such a way that beneath the protruding lower edges of the upper strips 35 of the triangular tube 32 are formed catalyst-free cavities extending along the entire length of guide element 31 , and under the protruding edges of the bottom wall 34 of the triangle tube 32 there are cavities 41 free from the catalyst, also extending along the entire length of the guide element 31. Supplied to the channels 39 of triangular tubes.32 each through the holes 36 and 38, the liquid is introduced into the narrowing and narrowest part of each passage, & between the adjacent guide elements,
    The side wall of a triangular trz / b-ki annular support element can be made of two strips oriented along the support element and located one relative to the other in such a way that the lower edge of the upper band protrudes, for the upper edge of the lower band, Under the protrusions — the lower — edge of the upper strip of the side wall of the triangular tube of the annular opone element — have openings through which additional liquid from the internal channel of the triangular tube is fed into the passage between the annular support element ohm and the adjacent guide member,
    The magnitude of the acute angle between the vertical straight and outer surfaces of the upper and lower strips forming the side wall of the triangular tube of the annular support member must be within 10 - D0.
    Each side wall of the triangular tubes can be formed not from two, but from 3-5 strips, oriented in the direction of the length of the guide element. In such a design, the lower edge of the strip forming the side wall of the triangular tube protrudes beyond the upper edge of the strip below. Similarly as described in the present case, additional liquid flows into the tapering part and into the narrowest part of the passage between the adjacent guide elements through the holes located below the protruding lower edges mi forming the side walls of the triangular tube strips,
    Each row of holes 25, 36 and 38 extending along the guide element can be at least partially replaced by a slot oriented along the length of the guide element
    The BQ time of the normal operation of the reactor can introduce additional liquid or gas necessary for the catalytic conversion. For example, as such an additional gas in the described process of catalytic conversion of sulfur-containing mineral
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    oils can be used - gaseous hydrogen. The amount of additional hydrogen introduced into the reactor must ensure the maintenance of the three. The ratio of the volumes of sulfur-containing mineral oil and hydrogen,
    In cases where the process of catalytic conversion of a liquid and / or gas is endothermic, as an additional process. the liquid or gas must be heated to the reactor. or a gas, such as water vapor, or a heated liquid, is necessary for the catalytic conversion. .
    When using liquid guide elements 31 in the reactor, they can be sucked into the upper channel of the triangular tube 32 through openings 36 and, after being biased with additional liquid, can be passed into the passages between adjacent guide elements through holes 38,
    In the reactor design shown in FIG. 1, the catalyst bed is supported by a supporting cone 6, however, instead of this cone, a perforated disk or wire mesh can be used in the reactor, the additional advantage of which is that they can function as a separator separating the catalyst from the liquid. The bed of the reactor 1 can also serve as a support for the catalyst bed. Separate inlet pipes can be used to feed the liquid and gas into the reactor.
    In the proposed reactor, two or more separate catalyst layers can be used, and at least one of the catalyst layers should have a grid of guide elements of the described construction.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    1, A device for the catalytic conversion of a liquid and / or gas, Jz, a vertical housing with connections for supplying a convertible liquid and a gas or a convertible gas and a liquid and a catalyst, inside which there are lattices in height,
    consisting of guide elements, made in the form of boxes with pipes for supplying additional liquid and forming 51 Cheazda are channels, tapering along the course of the stream, and pipes for output of the catalyst and waste liquid, that, in order to intensify the process due to uniform distribution of the liquid and catalyst, holes were made in the casing to allow the additional liquid to flow into the narrowing part of the channel or close to the narrowing parts of the channels, and the gratings are provided with supporting elements E under boxes and forming between themselves expandable along the flow channels communicating with the tapered part osnovnk channels.
    I
    2 o The device according to claim 1, characterized in that the boxes have a triangular shape in cross section, and the supporting elements are made in a cross section in the form of an inverted triangle, connected by a base with the base of the duct.
    3 „Device according to nn. 1 and 2, it is t there that the guide elements are provided with additional boxes made in the form of a trapezium, placed between the bases of the main boxes and the bases of the supporting elements, while the base of the main box is made with the overlapping of the upper base additional ductwork and openings for additional fluid exit are made on this overlap.,
    five . The device according to claim 2 or item 3,. characterized in that the large bases of the additional ducts are installed with overlapping of the bases of the supporting elements and have
    0 openings for exit additional. liquids located on this floor.
    5. The device according to PP, 1-4, t, t, is characterized by the fact that the control elements in the lattice are arranged in a checkerboard pattern with respect to the guide elements in
    neighboring lattice.
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    同族专利:
    公开号 | 公开日
    SG75190G|1990-11-23|
    JPS627434A|1987-01-14|
    KR870000096A|1987-02-16|
    CN86103973A|1986-12-17|
    JPH0755289B2|1995-06-14|
    CA1274852A|1990-10-02|
    AU579935B2|1988-12-15|
    GB8515398D0|1985-07-17|
    MX170862B|1993-09-21|
    US4693807A|1987-09-15|
    KR940000861B1|1994-02-03|
    PH24726A|1990-10-01|
    NZ216540A|1989-07-27|
    AR242512A1|1993-04-30|
    ZA864475B|1987-01-28|
    CN1005383B|1989-10-11|
    NL8601575A|1987-01-16|
    AU5888586A|1986-12-24|
    DE3665073D1|1989-09-21|
    ES8801698A1|1988-02-16|
    EP0212689A1|1987-03-04|
    EP0212689B1|1989-08-16|
    ES556090A0|1988-02-16|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
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    US3073875A|1957-02-15|1963-01-15|Belge Produits Chimiques Sa|Process for preparation of acetylene|
    DE1645864C3|1966-11-10|1978-04-13|Daizo Kunii|Plant for the production of olefins by thermal cracking of hydrocarbons in the fluidized bed process and process for the production of olefins using this plant|
    US3702237A|1970-07-02|1972-11-07|Universal Oil Prod Co|Hydrocarbon conversion apparatus|
    US3816603A|1972-08-21|1974-06-11|Exxon Research Engineering Co|Process for decomposing ammonium sulfate into ammonium bisulfate and ammonia|
    NL188079C|1974-02-08|1992-04-01|Shell Int Research|DEVICE FOR CATALYTIC TREATMENT OF HYDROCARBONS.|
    US3913242A|1974-09-11|1975-10-21|Gear Co M W|Preheater for grain dryer|
    JPS5350053A|1976-10-18|1978-05-08|Kouji Watanabe|Gas treatment apparatus|
    US4371335A|1981-04-17|1983-02-01|Paraho Corporation|Zone separator for multiple zone vessels|
    GB2101905B|1981-07-22|1984-06-27|Shell Int Research|Apparatus for contacting fluid with particulate solid material|
    GB8326856D0|1983-10-07|1983-11-09|Shell Int Research|Moving catalyst bed reactor|GB2177318B|1985-07-02|1989-01-18|Shell Int Research|Catalytic conversion of gas or liquid in a multitube reactor|
    GB8729555D0|1987-12-18|1988-02-03|Shell Int Research|Alkylation process|
    US5601797A|1992-08-10|1997-02-11|Glitsch, Inc.|Liquid-phase catalyst-assembly for chemical process tower|
    US5600052A|1994-05-02|1997-02-04|Uop|Process and apparatus for controlling reaction temperatures|
    US5525311A|1994-05-02|1996-06-11|Uop|Process and apparatus for controlling reaction temperatures|
    US5540899A|1994-12-22|1996-07-30|Uop|BI-directional control of temperatures in reactant channels|
    US5538700A|1994-12-22|1996-07-23|Uop|Process and apparatus for controlling temperatures in reactant channels|
    US7473405B2|2004-10-13|2009-01-06|Chevron U.S.A. Inc.|Fluid distribution apparatus for downflow multibed poly-phase catalytic reactor|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB858515398A|GB8515398D0|1985-06-18|1985-06-18|Catalytic conversion of liquid/gas|
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