GB2275480A - A process of changing the molecular structure of hydrocarbon feed - Google Patents
A process of changing the molecular structure of hydrocarbon feed Download PDFInfo
- Publication number
- GB2275480A GB2275480A GB9401905A GB9401905A GB2275480A GB 2275480 A GB2275480 A GB 2275480A GB 9401905 A GB9401905 A GB 9401905A GB 9401905 A GB9401905 A GB 9401905A GB 2275480 A GB2275480 A GB 2275480A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
- C01B3/26—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using catalysts
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/28—Moving reactors, e.g. rotary drums
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/12—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with discontinuously preheated non-moving solid catalysts, e.g. blast and run
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
- C10G9/18—Apparatus
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00085—Plates; Jackets; Cylinders
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
- C01B2203/0277—Processes for making hydrogen or synthesis gas containing a decomposition step containing a catalytic decomposition step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1247—Higher hydrocarbons
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- General Health & Medical Sciences (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The process uses a reactor 1 which comprises a reactor body 2 provided with a plurality of parallel passages 4 and two manifolds 6 and 7 having two separate segments 8, 9 and 10, 11, and comprises continuously rotating the reactor body about its central longitudinal axis 5; supplying to segment 8 of manifold 6 the hydrocarbon feed, allowing in the passages 4 the structure of components in the hydrocarbon feed to change to produce a product with simultaneous formation of carbon deposited on the walls of the passages, and removing the product from the corresponding first segment 10 of manifold 7; and combusting separately a fuel to produce hot flue gas, and supplying to the segment 11 of manifold 7 the hot flue gas, allowing the carbon to oxidize and removing the formed effluent from the segment 9 of the opposite manifold 6. <IMAGE>
Description
A PROCESS OF CHANGING THE MOLECULAR STRUCTURE
OF A HYDROCARBON FEED
The present invention relates to a process of changing the molecular structure of components of a hydrocarbon feed. There are several conversion processes known to change the molecular structure of components of a hydrocarbon feed. At first heavy hydrocarbons can be converted into lighter, more volatile hydrocarbons at elevated temperature (about 500 "C) and at elevated pressure (in the range of from 10 to 25 bar), this process is referred to as thermal cracking. An alternative of this process is catalytic cracking, wherein a suitable catalyst is used to increase the reaction rate. The feed for cracking can also be liquefied petroleum gas to produce olefins, or methane the produce hydrogen.
To improve the anti-knock characteristics of a gasoline fraction the gasoline fraction is subjected to a reforming process. A suitable reforming process is platforming wherein a platinum-containing catalyst is used to catalyze the reaction, the reaction conditions are temperature of about 500 "C and pressure in the range of from 10 to 50 bar. Steam can be added to the feed as a reactant, for example in the reaction of methane and steam to synthesis gas (a mixture of carbon monoxide and hydrogen), or to moderate the temperatures. A further process is dehydrogenation.
A by-product of such processes is carbon which is deposited on the catalyst and has to be removed from the catalyst. To remove carbon from the catalyst, the catalyst is removed from the reactor in which the conversion process is carried out and treated separately. Moreover, the conversion reactions are endothermic so that heat has to be supplied continuously to the reactor.
It is an object of the present invention to provide a simple continuous process wherein the reaction can take place, wherein carbon is removed and wherein heat is supplied to the reactor.
Applicant now found that the problems can be overcome when the process of changing the molecular structure of components of a hydrocarbon feed is carried out in a reactor which comprises a reactor body provided with a plurality of passages arranged parallel to the central longitudinal axis of the reactor body and two manifolds arranged at either end of the reactor body, wherein each manifold comprises at least two separate segments which communicate with the passages.
Thus the process according to the present invention of changing the molecular structure of components of a hydrocarbon feed in a reactor which comprises a reactor body provided with a plurality of passages arranged parallel to the central longitudinal axis of the reactor body and two manifolds arranged at either end of the reactor body, wherein each manifold comprises at least two separate segments which communicate with the passages, the process comprising the simultaneous steps of (a) continuously rotating the reactor body; about its central longitudinal axis relative to the stationary manifolds or continuously rotating the segments of the manifolds relative to the stationary reactor body; (b) supplying to the first segment of a manifold the hydrocarbon feed optionally with steam, allowing in the passages the structure of components in the hydrocarbon feed to change to produce a product with formation of carbon which is deposited on the walls of the passages, and removing the product from the corresponding first segment of the opposite manifold; and (c) oxidizing the deposited carbon and supplying heat to the reactor body.
A reactor with a rotating catalyst bed for treating exhaust gases is disclosed in Katalytische Abluftreinigung: Verfahrenstechnische Aufgaben und neue Lösungen, G. Eigenberger and U.
Nieken, Chem.-Ing.-Tech. 63 (1991) No. 8, pages 781-791. The publication does not disclose the application of such a rotating reactor for the conversion processes, wherein several steps can be carried out simultaneously.
The invention will now be described by way of example in more detail with reference to the enclosed drawings, wherein
Figure 1 shows schematically a partly longitudinal section of the reactor for carrying out the process according to the invention;
Figure 2 shows schematically a cross-section along the line
II-II of Figure 1;
Figure 3 shows schematically a partly longitudinal section of an alternative design of the reactor for carrying out the process according to the invention;
Figure 4 shows schematically a cross-section along the line
IV-IV of Figure 3; and
Figure 5 shows schematically a cross-section along the line V-V of Figure 3.
Reference is now made to Figures 1 and 2. The reactor 1 for carrying out the process according to the invention comprises a reactor body 2 provided with a plurality of passages 4 arranged parallel to the central longitudinal axis 5 of the reactor body 2.
The reactor 1 further comprises a manifold 6 arranged at one end of the reactor body 2 and a manifold 7 arranged at the opposite end of the reactor body 2. Each manifold 6 and 7 comprises a first segment 8 and 10 respectively and a second segment 9 and 11 respectively, the segments 8 and 9 are separated by separation plate 12 and the segments 10 and 11 are separated by separation plate 13.
The segments 8, 9, 10 and 11 are open to the reactor body 2 so that they communicate with the passages 4. Each segment is provided with an opening into which a conduit (not shown) opens, the openings are referred to with reference numerals 15, 16, 17 and 18.
The reactor body 2 is rotatably arranged about its central longitudinal axis 5. Bearings and drive means have not been shown.
During normal operation the reactor body 2 is continuously rotated about its central longitudinal axis 5 relative to the segments 8, 9, 10 and 11 of the stationary manifolds 6 and 7.
Simultaneously therewith a hydrocarbon feed is supplied to segment 8 of manifold 6 through opening 15. The feed enters into the passages 4 which communicate with segment 8 and in the passages the reaction is allowed to take place. As a result the molecular structure of hydrocarbons in the feed changes to produce the required product and carbon is formed which carbon is deposited on the walls of the passages 4. Product is removed from the corresponding segment 10 of the opposition manifold 7.
In this way product is formed and carbon is deposited in the passages 4 pertaining to one half of the reactor body 2. Carbon is removed from the passages pertaining to the other other half of the reactor body 2 and heat is supplied to the reactor body 2.
To this end a fuel is separately combusted to produce hot flue gas which is supplied to segment 11 of manifold 7. The hot flue gas passes through the passages 4 of the reactor body 2. This hot flue gas contains sufficient free oxygen to oxidize the carbon which is present on the walls of the passages 4. Formed effluent is removed from the corresponding segment 9 of the opposite manifold 6.
A conversion which can be carried out with the above process is the reaction of methane and steam to synthesis gas. The reactor body 2 is continuously rotated. Simultaneously therewith a feed of methane and steam is supplied at a pressure in the range of from 3 to 8 bar to segment 8 of manifold 6 through opening 15. The feed enters into the passages 4 which communicate with segment 8 and in the passages the reaction is allowed to take place. Synthesis gas is removed from the corresponding segment 10 of the opposition manifold 7. Some carbon is formed and deposited in the passages 4 pertaining to one half of the reactor body 2. A fuel is separately combusted to produce hot flue gas which is supplied to segment 11 of manifold 7. The hot flue gas passes through the passages 4 of the reactor body 2. This hot flue gas contains about 2 to 5 %vol.
of free oxygen which is sufficient to oxidize the carbon which is present on the walls of the passages 4. Formed effluent is removed from the corresponding segment 9 of the opposite manifold 6. The hot flue gas heats the reactor body 2 to about 1 550 "C.
The process can also be used for catalytic reforming, which conversion includes dehydrogenation, hydrocracking, cyclization and isomerization of naphtha fractions. The conversion can suitably be carried out in two stages, a first stage, wherein a feed of naphtha fractions is passed through a first rotating reactor body for the endothermic dehydrogenation and cyclization stage at a pressure in the range of from 5 to 20 bar, the reactor body is heated with flue gas to about 600 "C, and the intermediate product leaving the reactor body has a temperature of about 500 "C. This intermediate product is supplied to a second rotating reactor body heated to about 500 "C with the flue gas used to heat the first reactor, and in the second reactor intermediate product from the first reactor is hydrocracked and isomerized.
The process can further be used for manufacturing ethylene by cracking naphtha, wherein a feed of naphtha and steam is supplied to a rotating reactor body heated with hot flue gas to a temperature in the range of from 800 to 900 "C. The steam to hydrocarbon ratio in the feed is in the range of from 0.5 to 0.8.
This process is applicable for those conversion processed where little carbon is formed. There are other processes, such as cracking of methane wherein methane is converted to hydrogen and carbon and wherein a large amount of carbon is deposited on the walls of the passages. This carbon can be removed with steam according to the reaction carbon with steam gives hydrogen and carbon monoxide, the latter gas mixture being referred to as synthesis gas.
Reference is now made to Figures 3, 4 and 5. The reactor 1' for carrying out the process according to the invention comprises the reactor body 2 provided with a plurality of passages 4 arranged parallel to the central longitudinal axis 5 of the reactor body 2.
The reactor 1' further comprises a manifold 6' arranged at one end of the reactor body 2 and a manifold 7' arranged at the opposite end of the reactor body 2. The first manifold 6' comprises a first segment 30, a second segment 33, and a third segment 34. The second manifold 7' also comprises three segments corresponding to the segments of the first manifold 6', the segments are referred to by reference numerals 35, 36 and 37. The segments of the first manifold 6' are separated by separation plates 40 and the segments of the second manifold 7' are separated by separation plates 41.
The segments have substantially equal areas, Each segment of the manifolds 6' and 7' is provided with an opening into which a conduit (not shown) opens, the openings in the segments of the first manifold 6' are referred to with reference numerals 51, 52 and 53, and the openings in the segments of the second manifold 7' are referred to by reference numerals 54, 55 and 56.
During normal operation the reactor body 2 is continuously rotated about its central longitudinal axis 5 relative to the segments of the stationary manifolds 6' and 7'.
Simultaneously therewith a hydrocarbon feed is supplied to segment 30 of manifold 6' through opening 51. The feed enters into the passages 4 which communicate with segment 30 and in the passages the reaction is allowed to take place. As a result the molecular structure of hydrocarbons in the feed changes to produce the required product and carbon is formed which carbon is deposited on the walls of the passages 4. Product is removed from the corresponding segment 35 of the opposition manifold 7' through opening 54.
In this way product is formed and carbon is deposited in the passages 4 pertaining to one third of the reactor body 2. Carbon is removed from the passages pertaining to the other two thirds of the reactor body 2 and heat is supplied to the reactor body 2.
To this end steam is supplied to the second segment 36 of manifold 7', the steam is allowed to enter into the passages 4 of the reactor body 2 and it reacts with carbon to form synthesis gas which is removed from the corresponding second segment 33 of the opposite manifold 6'. Simultaneously a fuel is separately combusted to produce hot flue gas. The hot flue gas is supplied to the third segment 34 of manifold 6' and it is allowed to pass through the passages 4 of the remaining part of the reactor body 2 to heat the reactor body 2, cooled flue gas is removed from the corresponding third segment 37 of the opposite manifold 7'.
As observed above, cracking of methane involves the reaction of methane to carbon and hydrogen, and the reaction of carbon with steam to carbon monoxide and hydrogen to remove deposited carbon. A feed comprising methane is supplied to segment 30 of manifold 6' through opening 51. The feed enters into the passages 4 of the rotating reactor body 2 which communicate with segment 30 and in the passages the reaction to carbon and hydrogen is allowed to take place. Hydrogen is removed from the corresponding segment 35 of the opposition manifold 7' through opening 54. The formed carbon is deposited in the passages 4 pertaining to one third of the reactor body 2.Steam is supplied to the second segment 36 of manifold 7', the steam is allowed to enter into the passages 4 of the reactor body 2 and it reacts with carbon to form synthesis gas which is removed from the corresponding second segment 33 of the opposite manifold 6'. Simultaneously a fuel is separately combusted to produce hot flue gas. The hot flue gas is supplied to the third segment 34 of manifold 6' and it is allowed to pass through the passages 4 of the remaining part of the reactor body 2 to heat the reactor body 2 to a temperature in the range of from 1 250 to 1 400 "C, cooled flue gas is removed from the corresponding third segment 37 of the opposite manifold 7'.
The reactor as described with reference to Figures 3-5 can also be used for a two stage conversion process such as the above described catalytic reforming. Then the reactor body 2 is continuously rotated about its central longitudinal axis 5 relative to the segments of the stationary manifolds 6' and 7'. Simultaneously therewith a hydrocarbon feed is supplied to segment 30 of manifold 6' through opening 51. The feed enters into the passages 4 which communicate with segment 30 and in the passages the reaction is allowed to take place. As a result the molecular structure of hydrocarbons in the feed changes to produce an intermediate product and carbon is formed which carbon is deposited on the walls of the passages 4. Intermediate product is removed from the corresponding segment 35 of the opposition manifold 7' through opening 54. The intermediate product is supplied to the second segment 36 of manifold 7', and allowed to enter into the passages 4 of the reactor body 2 where it reacts to form the required product which is removed from the corresponding second segment 33 of the opposite manifold 6'. Simultaneously a fuel is separately combusted to produce hot flue gas. The hot flue gas is supplied to the third segment 34 of manifold 6' and it is allowed to pass through the passages 4 of the remaining part of the reactor body 2 to heat the reactor body 2, cooled flue gas is removed from the corresponding third segment 37 of the opposite manifold 7'.
The fuel can be a separate fuel, or it can include part of the product formed or part of the synthesis gas formed when carbon is oxidized with steam.
In the reactor described with reference to Figures 1 through 5 the reactor body rotated relative to stationary manifolds, it will be understood that in an alternative design of the reactor the manifolds rotate relative to a stationary reactor body.
In the designs shown in Figures 1 and 3 the corresponding segments were arranged directly opposite to each other, in practice they will be arranged rotated with respect to each other over a fixed angle, the magnitude of the angle being the angular rotation of the reactor body relative to the manifolds for the time it takes for gas to pass through the passages from one end of the reactor body to the other.
The reactor body can be a monolith or a honeycomb wherein the passages are parallel to the central longitudinal axis of the reactor body, or the reactor body can consists of a plurality of parallel pipes or rods. When the particular process requires catalytically active material such material can be deposited in the passages.
In the designs shown in the Figures the areas of the segments of each manifold are substantially equal in size, however, when the amount of fluid for one of the steps is large in comparison to the amount of the fluid in the other step the magnitudes of the areas of the segments through which the fluids are supplied and can be adjusted so that the areas have different sizes, this applies as well to the areas of the corresponding segments of the opposite manifold.
It will be understood that more than three segments per manifold can be applied as well should the process require so.
For a catalytic conversion process the passages can be provided in a known manner with suitable catalytic material.
Claims (7)
1. Process of changing the molecular structure of components of a hydrocarbon feed in a reactor which comprises a reactor body provided with a plurality of passages arranged parallel to the central longitudinal axis of the reactor body and two manifolds arranged at either end of the reactor body, wherein each manifold comprises at least two separate segments which communicate with the passages, which process comprises the simultaneous steps of (a) continuously rotating the reactor body about its central longitudinal axis relative to the stationary manifolds or continuously rotating the segments of the manifolds relative to the stationary reactor body;; (b) supplying to the first segment of a manifold the hydrocarbon feed optionally with steam, allowing in the passages the structure of components in the hydrocarbon feed to change to produce a product with formation of carbon which is deposited on the walls of the passages, and removing the product from the corresponding first segment of the opposite manifold; and (c) oxidizing the deposited carbon and supplying heat to the reactor body.
2. Process according to claim 1, wherein each manifold comprises two segments, and wherein step (c) comprises combusting separately a fuel to produce hot flue gas; and supplying to the second segment of a manifold the hot flue gas, allowing the carbon to oxidize and removing the formed effluent from the corresponding second segment of the opposite manifold.
3. Process according to claim 1, wherein each manifold comprises three segments, and wherein step (b) comprises supplying to the first segment of a manifold the hydrocarbon feed optionally with steam, allowing in the passages the structure of components in the hydrocarbon feed to change to produce an intermediate product, removing the intermediate product from the corresponding first segment of the opposite manifold, supplying to the second segment of a manifold the intermediate product, allowing in the passages the structure of components in the hydrocarbon feed to change to produce a product, and removing the product from the corresponding second segment of the opposite manifold, and wherein step (c) comprises combusting separately a fuel to produce hot flue gas; and supplying to the third segment of a manifold the hot flue gas, allowing deposited carbon to oxidize and removing the formed effluent from the corresponding third segment of the opposite manifold.
4. Process according to claim 1, wherein each manifold comprises three segments, and wherein the step of oxidizing the deposited carbon and supplying heat to the reactor body comprises supplying steam to the second segment of a manifold, allowing the steam to react with the carbon to produce synthesis gas and removing synthesis gas from the corresponding second segment of the opposite manifold; combusting separately a fuel to produce hot flue gas; and supplying to the third segment of a manifold hot flue gas to heat the reactor body and removing cooled flue gas from the corresponding third segment of the opposite manifold.
5. Process according to claim 3 or 4, wherein the hydrocarbon feed consists of higher hydrocarbons and wherein the product is hydrogen.
6. Process according to claim 3 or 4, wherein the hydrocarbon feed consists of methane and wherein the product is hydrogen.
7. Process according to anyone of the claims 1-4, wherein the hydrocarbon feed consists of heavier hydrocarbons and wherein the product includes olefins and/or aromatics.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP93200275 | 1993-02-03 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB9401905D0 GB9401905D0 (en) | 1994-03-30 |
| GB2275480A true GB2275480A (en) | 1994-08-31 |
Family
ID=8213605
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB9401905A Withdrawn GB2275480A (en) | 1993-02-03 | 1994-02-01 | A process of changing the molecular structure of hydrocarbon feed |
Country Status (1)
| Country | Link |
|---|---|
| GB (1) | GB2275480A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL1003504C2 (en) * | 1996-07-04 | 1998-01-07 | Univ Delft Tech | Rotary reactor and application thereof. |
| WO1999016544A1 (en) * | 1997-10-01 | 1999-04-08 | Imperial Chemical Industries Plc | Exothermic process |
| WO1999016543A1 (en) * | 1997-10-01 | 1999-04-08 | Imperial Chemical Industries Plc | Endothermic process |
| EP1630129A1 (en) * | 2004-08-25 | 2006-03-01 | The Boc Group, Inc. | Hydrogen production process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1148592A (en) * | 1966-04-07 | 1969-04-16 | Sun Oil Co | Shock tube reactors and their operation |
| US4952374A (en) * | 1986-06-19 | 1990-08-28 | Atlantic Richfield Company | Rotating catalyst bed with pressurized gas seal for methane conversion system |
-
1994
- 1994-02-01 GB GB9401905A patent/GB2275480A/en not_active Withdrawn
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1148592A (en) * | 1966-04-07 | 1969-04-16 | Sun Oil Co | Shock tube reactors and their operation |
| US4952374A (en) * | 1986-06-19 | 1990-08-28 | Atlantic Richfield Company | Rotating catalyst bed with pressurized gas seal for methane conversion system |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL1003504C2 (en) * | 1996-07-04 | 1998-01-07 | Univ Delft Tech | Rotary reactor and application thereof. |
| WO1998001222A1 (en) * | 1996-07-04 | 1998-01-15 | Technische Universiteit Delft | Rotary reactor and use thereof |
| WO1999016544A1 (en) * | 1997-10-01 | 1999-04-08 | Imperial Chemical Industries Plc | Exothermic process |
| WO1999016543A1 (en) * | 1997-10-01 | 1999-04-08 | Imperial Chemical Industries Plc | Endothermic process |
| US6291686B1 (en) | 1997-10-01 | 2001-09-18 | Imperial Chemical Industries Plc | Exothermic process |
| EP1630129A1 (en) * | 2004-08-25 | 2006-03-01 | The Boc Group, Inc. | Hydrogen production process |
| US7544342B2 (en) | 2004-08-25 | 2009-06-09 | The Boc Group, Inc. | Hydrogen production process |
Also Published As
| Publication number | Publication date |
|---|---|
| GB9401905D0 (en) | 1994-03-30 |
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