KR20170082186A - Self heat supply dehydrogenation reactor for inducing isothermal reaction - Google Patents
Self heat supply dehydrogenation reactor for inducing isothermal reaction Download PDFInfo
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- KR20170082186A KR20170082186A KR1020160001056A KR20160001056A KR20170082186A KR 20170082186 A KR20170082186 A KR 20170082186A KR 1020160001056 A KR1020160001056 A KR 1020160001056A KR 20160001056 A KR20160001056 A KR 20160001056A KR 20170082186 A KR20170082186 A KR 20170082186A
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- dehydrogenation
- catalyst
- catalytic combustion
- column
- reactor
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- 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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
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- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
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- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/72—Copper
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- 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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
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- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a fuel cell system, which comprises a housing defining an interior of a reactor, a housing having a feed gas inlet formed at an upper side thereof and a reaction gas outlet formed at a lower portion thereof, a catalyst coaxially disposed inside the housing, A first catalytic combustion column which is filled with a dehydrogenating material and which is coaxially arranged with the catalytic combustion column inside the catalytic combustion column and which is filled with a dehydrogenation catalyst and which passes through the catalytic combustion column A dehydrogenation catalyst layer in which a dehydrogenation reaction proceeds and a second catalytic combustion column disposed in a space inside the dehydrogenation catalyst layer and coaxially disposed with the dehydrogenation catalyst layer and having a self- The present invention relates to a dehydrogenation reactor for heat supply, By using a small column to supply heat required for the dehydrogenation process, and induction so that the entire process can be isothermal reaction by applying a system of its own supply of additional heat to the reactor it can be improved dehydrogenation performance.
Description
The present invention relates to a dehydrogenation reactor useful for dehydrogenating various hydrocarbon raw materials, and more particularly, to a dehydrogenation reactor useful for dehydrogenating various hydrocarbons by using a catalytic combustion column, The present invention relates to a dehydrogenation dehydrogenation reactor.
The dehydrogenation of propane with propylene and isobutane with isobutene produces olefins which are more reactive than alkane feedstocks and which are easy to form coke at high temperatures used for dehydrogenation. The dehydrogenation reactor is a very large, long columnar vertical structure with a diameter of about 5 to 30 feet and a length of 10 to 100 feet or more. The general structure of this reactor is to inject a reactive gas into the inlet located at the bottom center of the vertical reactor where the gas flows up through the annular zone and passes radially outward through a porous catalyst bed or other suitable dehydrogenation catalyst Passes upwardly through the outer annular zone to be discharged from the top of the reactor outer part. These reactors are often referred to as "radial" reactors because the reactant gas flow through the catalyst bed is radial.
Generally, the radial flow reaction zone consists of cylindrical zones having various nominal cross-sectional areas, which are arranged vertically and coaxially to form reaction zones. Typically, the radial flow reaction zone includes a cylindrical reaction vessel having a cylindrical outer catalyst containing screen and a cylindrical inner catalyst containing screen coaxially disposed with the reaction vessel. The inner screen has a nominal inner cross-sectional area smaller than the outer screen and has a nominal inner cross-sectional area smaller than the reaction vessel. The reaction gas stream is introduced into an annular space present between the inner wall of the reaction vessel and the outer surface of the outer screen. The reactive gas stream flows radially through an annular space existing between the outer screen and the inner screen through the outer screen and then through the inner screen. The collected stream into the cylindrical space inside the inner screen is withdrawn from the reaction vessel.
The propane dehydrogenation process is based on an endothermic reaction and sufficient energy must be supplied during the reaction process in order for the reaction to proceed properly. Various techniques have been developed and applied in practice as an energy source for the propane dehydrogenation process, and the most common method is a fired heater. The furnace is installed upstream of the reactor to supply a certain amount of energy for the dehydrogenation process of the endothermic reaction. Propane, which is the main reaction gas, is injected into the high temperature heating furnace together with hydrogen before being introduced into the catalytic reactor, and is heated to a proper temperature through a heat exchange process.
1 is a schematic diagram showing a general dehydrogenation system in which heat is supplied using a heating furnace. Referring to FIG. 1, propane and hydrogen, which are reaction gases, pass through a heating furnace, are subjected to a heat exchange and heating process, and then are injected into a dehydrogenation catalytic reactor. Conventionally, in a heating furnace used as a preheating device, a supply gas is supplied to a U-shaped pipe, and a plurality of burners are disposed around the pipe to heat the pipe. Since the heating furnace having such a structure can be heated at a high temperature of 600 to 700 ° C. or higher, it is suitable as a preheating device for the dehydrogenation process, but it is difficult to control the temperature and has a high risk in a process using a combustible gas. In addition, selective heating is not possible depending on the reactor location and section, and a temperature gradient is generated between the inside and the outside of the propane pipe, and locally heated portions are generated. As a result, thermal cracking is a side reaction. This side reaction is one of the most important parameters to control the heating condition of the furnace because it decreases the yield of propylene and is the main cause of reduction of the process performance. Therefore, there is a problem that an enormous initial investment cost and maintenance cost for insulation treatment of the pipe connecting the heating furnace and the reactor occur.
On the other hand, Korean Patent Application No. 10-2006-0119537 discloses a module type integral type reformer device capable of simultaneously performing an exothermic reaction for supplying heat using catalytic combustion and an endothermic reaction for producing hydrogen. However, the prior art document differs from the present invention in that it is a device for a hydrogen reformer, and in particular, the prior art is directed to an indirect heat exchange between a catalyst exothermic reaction and a hydrogen reformer reaction, There is a difference in that the raw material gas is heated.
In order to overcome the problems of the prior art described above, the object of the present invention is to provide a catalyst combustion column comprising a catalyst that generates heat during the catalytic reaction, and by supplying the energy required for the endothermic reaction in the propane dehydrogenation process, Temperature reaction so that the process yield can be improved and the cost of operation, maintenance and repair can be reduced.
According to an aspect of the present invention, there is provided a method of manufacturing a semiconductor device, the method comprising the steps of: providing a housing defining an interior of the reactor, having a raw material gas inlet formed at an upper surface thereof and a reaction gas outlet formed at a lower portion thereof; A first catalyst combustion column arranged in the form of a coaxial phase and filled with a catalyst having self-heating characteristics to heat the raw material gas; a first catalyst combustion column arranged inside the catalytic combustion column coaxially with the catalytic combustion column A dehydrogenation column in which a dehydrogenation column is filled with a dehydrogenation catalyst and a dehydrogenation reaction of a raw material gas passing through the catalyst combustion column proceeds, and a dehydrogenation column disposed in an inner space of the dehydrogenation catalyst layer and disposed coaxially with the dehydrogenation catalyst layer, And a second catalytic combustion column (second catalytic combustion chamber) catalyst combustion column). < / RTI >
The self heat supply dehydrogenation reactor according to the present invention is a system for supplying heat required in the dehydrogenation process and supplying additional heat to the inside of the reactor by using a catalytic combustion column that generates heat by itself, . As a result, there is no point locally heated in the reactor and the temperature gradient between the inside / outside of the reactor and the inside / outside of the reactor is small, so that heat cracking of the propane can be prevented and the yield of the dehydrogenation process can be increased. In addition, the manufacturing cost can be reduced by reducing the reaction temperature reduction problem and the heat insulation treatment cost due to the heat loss of the piping and the reactor. In addition, since the pressure applied to the catalyst is reduced, not only the process problems due to the catalyst breakage are reduced, but also the catalyst loss can be reduced, so that the overall operation cost can be saved.
1 is a schematic diagram showing a general dehydrogenation system in which heat is supplied using a heating furnace.
FIG. 2 is a schematic longitudinal sectional view of a self-heat supplying dehydrogenation reactor according to an embodiment of the present invention. FIG.
3 is a partial perspective view of a catalytic combustion column according to an embodiment of the present invention.
4 is a partial perspective view illustrating self-exothermic catalyst particles around a raw material injection pipe and a raw material injection pipe according to an embodiment of the present invention.
The present invention will now be described in more detail with reference to the accompanying drawings. Although the terms used in the present invention have been selected as general terms that are widely used at present, there are some terms selected arbitrarily by the applicant in a specific case. In this case, the meaning described or used in the detailed description part of the invention The meaning must be grasped. Like reference numerals refer to like elements throughout the specification.
Although the drawings illustrate specific shapes of the dehydrogenation reactor of the present invention, such a dehydrogenation reactor may have various shapes suitable for the specific environment in which it is performed in a particular application, And the like. Moreover, the numbers in the figures represent a simple schematic diagram of the dehydrogenation reactor of the present invention, only major components being shown. Other pumps, moving pipes, valves, hatches, access outlets and other similar components have been omitted.
The use of these components to modify the described dehydrogenation reactor is well known to those skilled in the art and does not depart from the scope and spirit of the appended claims.
As used herein, the term "fluid" means a gas, liquid, or gas or liquid containing a dispersed solid or a mixture thereof. The fluid may be in the form of a gas containing dispersed droplets.
As used herein, the term "reaction zone" means the space in the dehydrogenation reactor where the reaction gas is in contact with the catalyst on the catalyst bed.
Here, the direction of the flow of solids through the device in the downward or gravitational direction, that is to say through the cross-flow gas, is oriented, so the use of the terms 'downward' and 'upward' is relative to the direction of the gravitational direction.
As used herein, the term " inner "or" inner "refers to the direction of the radial center of the circle, which is the cross-section perpendicular to the direction of gravity of the annular reactor.
As used herein, the term " outer "or" outer "refers to the direction of the radial circumference of the circle, which is a section cut perpendicular to the gravitational direction of the annular reactor.
The term "screen " herein has a broad meaning, including means suitable for limiting the catalyst to the catalyst bed while permitting flow of the reaction gas stream across the catalyst bed.
The numbers in the figures represent a simplified schematic diagram of the dehydrogenation reactor according to the invention, only the main components being shown. Other pumps, moving pipes, valves, hatches, access outlets, and other similar components have been omitted. The use of these accessories to modify the dehydrogenation reactor described is well known to those skilled in the art and does not depart from the scope and spirit of the appended claims.
FIG. 2 is a schematic longitudinal sectional view of a self-heat supplying dehydrogenation reactor according to an embodiment of the present invention. FIG. Referring to FIG. 2, the self-heat supplying
And a second catalytic combustion column (40) disposed coaxially with the dehydrogenation catalytic layer (30) in the inner space of the dehydrogenation catalytic layer (30) and heating a raw material gas by filling a self exothermic catalyst .
The
The first
The second
The
The first
The raw material gas is injected into the
The dehydrogenation catalyst layer 30 has a
The second
A reaction
3 is a partial perspective view of a catalytic combustion column according to an embodiment of the present invention. Referring to FIG. 3, the interior of the first and second
In an embodiment of the present invention, the distance d between adjacent raw
A raw material
4 is a partial perspective view illustrating self-exothermic catalyst particles around a raw material injection pipe and a raw material injection pipe according to an embodiment of the present invention. Referring to FIG. 4, self-
In the present invention, as a catalyst having a self-heating property, a metal generally selected from the group consisting of platinum (Pt), palladium (Pd), rhodium (Rh), gold (Au), copper (Cu) The catalysts may be used alone or in combination. The catalyst preferably has a particle size in the range of 1.0 to 2.0 mm, more preferably in the range of 1.5 to 1.7 mm.
According to the present invention, it is possible to selectively heat according to the position and the interval of the
In the self-heat supplying
INDUSTRIAL APPLICABILITY As described above, the self-heat supplying dehydrogenation reactor according to the present invention is characterized in that the first catalytic combustion column and the second catalytic combustion column are applied so that there is no locally heated point and the temperature gradient between the inside / It is possible to reduce the production cost by reducing the reaction temperature reduction problem and the heat insulation treatment cost due to the heat loss of the piping and the reactor .
While the invention has been described in connection with various specific embodiments, it is to be understood that various modifications thereof will become apparent to those of ordinary skill in the art upon reading the specification. Accordingly, the invention as described herein is intended to embrace such modifications as fall within the scope of the appended claims.
10: housing 11: source gas inlet
12: reaction gas outlet 20: first catalyst heating column
30: dehydrogenation catalyst layer 31: catalyst distribution pipe
32: catalyst outlet pipe 33: outer screen
34: inner screen 35: dehydrogenation catalyst particle
40: second catalyst heating column 50: reaction gas collecting region
60: feed pipe 61: self-heating catalyst
62: catalyst bed 63: raw material injection screen
Claims (14)
An annular first catalyst heating column disposed inside the housing coaxially with a longitudinal central axis of the housing and having a self-heating catalyst having self-heating characteristics filled therein to heat the source gas;
A dehydrogenation catalyst layer disposed coaxially with the first catalyst heating column inside the first catalyst heating column and being filled with a dehydrogenation catalyst therein so that the dehydrogenation reaction of the feed gas passing through the first catalyst heating column proceeds; And
And a second catalytic combustion column which is disposed coaxially with the dehydrogenation catalyst layer in the inner space of the dehydrogenation catalyst layer and is filled with a self exothermic catalyst having self- Reactor.
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KR1020160001056A KR101831507B1 (en) | 2016-01-05 | 2016-01-05 | Self heat supply dehydrogenation reactor for inducing isothermal reaction |
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Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN114011344A (en) * | 2021-12-03 | 2022-02-08 | 嘉兴京能科技有限责任公司 | Supercharging device is collected in organic matter catalytic dehydrogenation |
CN114251653A (en) * | 2021-12-23 | 2022-03-29 | 大连大学 | Catalytic combustion hydrogen storage and release device and method |
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FR2817172B1 (en) * | 2000-11-29 | 2003-09-26 | Inst Francais Du Petrole | CHEMICAL CONVERSION REACTOR OF A LOAD WITH HEAT SUPPLIES AND CROSS CIRCULATION OF THE LOAD AND A CATALYST |
JP2005145756A (en) * | 2003-11-14 | 2005-06-09 | Sekisui Chem Co Ltd | Dehydrogenation method |
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN114011344A (en) * | 2021-12-03 | 2022-02-08 | 嘉兴京能科技有限责任公司 | Supercharging device is collected in organic matter catalytic dehydrogenation |
CN114011344B (en) * | 2021-12-03 | 2024-03-22 | 嘉兴京能科技有限责任公司 | Supercharging device is collected in organic matter catalytic dehydrogenation |
CN114251653A (en) * | 2021-12-23 | 2022-03-29 | 大连大学 | Catalytic combustion hydrogen storage and release device and method |
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