CA1209943A - Procedure for thermal cracking of hydrocarbon oils - Google Patents
Procedure for thermal cracking of hydrocarbon oilsInfo
- Publication number
- CA1209943A CA1209943A CA000429300A CA429300A CA1209943A CA 1209943 A CA1209943 A CA 1209943A CA 000429300 A CA000429300 A CA 000429300A CA 429300 A CA429300 A CA 429300A CA 1209943 A CA1209943 A CA 1209943A
- Authority
- CA
- Canada
- Prior art keywords
- pressure vessel
- fluid
- helix
- reaction zone
- gas mixture
- 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.)
- Expired
Links
- 238000000034 method Methods 0.000 title claims abstract description 29
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 20
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 20
- 238000004227 thermal cracking Methods 0.000 title claims abstract description 10
- 239000003921 oil Substances 0.000 title description 10
- 239000004215 Carbon black (E152) Substances 0.000 title description 8
- 238000006243 chemical reaction Methods 0.000 claims abstract description 43
- 239000000203 mixture Substances 0.000 claims abstract description 22
- 239000012530 fluid Substances 0.000 claims abstract description 21
- 208000036366 Sensation of pressure Diseases 0.000 claims 2
- 238000004140 cleaning Methods 0.000 abstract description 3
- 238000005336 cracking Methods 0.000 description 19
- 239000007789 gas Substances 0.000 description 13
- 239000007788 liquid Substances 0.000 description 4
- 239000000543 intermediate Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 230000007423 decrease Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 241000252095 Congridae Species 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 241000428533 Rhis Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000010771 distillate fuel oil Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000010763 heavy fuel oil Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000002706 hydrostatic effect Effects 0.000 description 1
- 230000007775 late Effects 0.000 description 1
- -1 petrol Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 230000002250 progressing effect Effects 0.000 description 1
- 230000036647 reaction Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
Classifications
-
- 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
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00823—Mixing elements
- B01J2208/00831—Stationary elements
- B01J2208/0084—Stationary elements inside the bed, e.g. baffles
-
- 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
- B01J2219/00761—Details of the reactor
- B01J2219/00763—Baffles
- B01J2219/00765—Baffles attached to the reactor wall
- B01J2219/0077—Baffles attached to the reactor wall inclined
- B01J2219/00772—Baffles attached to the reactor wall inclined in a helix
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
In a process for the thermal cracking of hydrocarbons, the hydrocarbons are heated to reaction temperature and conducted into the reaction zone, where the flow is upward from below. The fluid/gas mixture is set in tangential rotation in the pressure vessel by means of a helix system or by nozzles. A uniform delay time is obtained without the need for intermediate plates which impede cleaning operations.
In a process for the thermal cracking of hydrocarbons, the hydrocarbons are heated to reaction temperature and conducted into the reaction zone, where the flow is upward from below. The fluid/gas mixture is set in tangential rotation in the pressure vessel by means of a helix system or by nozzles. A uniform delay time is obtained without the need for intermediate plates which impede cleaning operations.
Description
~2~9943 'rhis inve~tion relates to a process for the thermal cracking of hydrocarbon oils, in which process the hydrocarbons are heated to reaction temperature and conducted into a reaction zone, where the ~low is l~pward from below.
In ~he the~ïrlal cracking of hydrocarbon oils, heavy oil frlcti~ns are cracked to lighter fractions to increase the yield of the latter. In the cracking process, the Eeed oil is heated in the heating tubes of the cracking furnace to cracking tempera-ture. As a rule, two alternative methods are available. In one of them, cracking takes place in the heating tubes of the crackinq furnace and partly in the pipelines which lead to the process steps following the cracking. In this cracking process the delay times are not exactly known, but they are relatively short, in the order of one minute. The pressure varies greatly, going down from the furnace entrance to the furnace exit. In the other cracking process, the hydrocarbon feed is first heated in the cracking furnace to a suitable reaction temperature, and the actual cracking reaction takes place in a separate reaction zone, where the delay time is considerably lon~er than in the preceding process, that is, in the order of 10 to 30 minutes. No heat is introduced to the reaction zone.
In the last-mentioned process, the reaction zone as a rule consists of an upright, cylindrical pressure vessel, at one end of which the oil feed heated in the cracking furnace is in-troduced and at the other end of which extracted a mixture of liquid and gas to go to further refining steps extracted, for in-stance for distillation. The flow direction in the reaction One has been either downward from above or upward from helow.
In the thermal cracking of hydrocarbon oils, reactions of substantiall~ two kinds take place. One of them is the crack-ing reaction proper, the long-chain molecules being split into smaller molecules, causing reduction of viscosity. The other ., ,j'~l" '~
~Z~9g~3 - reactlon type is called polycondensati~n, whereby the molecules combine and prod~ce pitch and coke as hydrogen is set free. The last-mentioned reaction is an undesired reaction because it re-sults in greater quantities of asphaltelles. Since the condensing reac~ions grow to be signiEicant al hi~ er telllL~(-rat~lres, cn~ea-vours ace made to use lower reactio~ cm~ rt~ Lcs ~nd c~rrc~ )olld-ingly lon~er delay times.
The delay time is very important for thermal cracking.
The cracking has not time to ta~e place if the delay time is too lG short. In a case where the delay time is too long, the cracking products begin to react and to form undesired reaction products.
As a result, an unstable product is formed which causes difficul-ties in the further use of fuel. The aim is therefore to achieve a cracking as uniform as possible. If the flows in the pressure vessel serving as reaction zone are non-uniform, the result will be varying delay times.
In the cracking reaction, light components are formed which evaporate at the temperature and pressure in the reaction zone. Therefore, the density of the liquid/gas mixture decreases as the mixture flows upward in the pressure vessel. Owing to the ~ hydrostatic pressure differential in the pressure vessel, the density of the gas part also decreases as the mixture flows up-ward. The liquid fractions formed in the cracking reactor have a lower density than the feed, which also lowers the density of the liquid/gas mixture. Therefore, the flow velocity is not con-stant in the usually employed cylindrical reactor with uniform thickness, but accelerates as the mixture flows upward.
The thermal cracking procedure disclosed in U~S. Patent No. 4,2~7,387 has a cylindrical vertical pressure vessel serving as reaction zone. With a view to preventing refluxes within the reactor, perforated intermediate plates are provided at the bottom of the reaction zone to form a plurality of mixing sites in the ~09943 reactor. The object is to achievc a delay time as uniform as possible for the fraction fed into the zone. The use of inter-mediate plates has its drawbacks. ~aulty operation of the reac-tor may ca~lse the who]e reactor to be coked to occlusion. The intermeclilte l~lates rnake the co~e removal and reactor cleaning inconvc~ ier~t ~nd e~pensive.
~ n object of the invention is to achieve an in~E~rov~mellt in the processes known in the art. A more ~etailed object of the invention is to provide a process in which a uniform delay time can be attained without the need for intermediate plates that hamper the cleaning process.
According to the present invention there is provided a process for the thermal crac~ing of hydrocarbons, wherein the hydrocarbons are heated to reaction temperature and conducted into a reaction zone as a fluid/gas mixture, where the flow is upwards from below, and wherein the fluid/gas mixture is set in tangential rotation in a pressure vessel defining the reaction zone.
A tangentially rotating, but vertically uniformly up-wards progressing fluid/gas flow with no return flows causing non-uniform delay times is generated in the reaction zone.
The tangentially rotating flow of the fluid/gas mixture can be obtained in a number of ways. In a preferred embodiment, the rotary motion is produced by means of helical members that form a helically ascending corridor in the pressure vessel serv-ing as reactor. In this passage, the f~ow is always in the up-wards direction and no downflows occur. The helix system may extend over the entire length of the reaction zone, or only over part of it. In some instances, it may suffice to restrict the helix system to the entrance section of the reaction zone.
It is also possible to provide in the reactor two or more helix-like members, which reverse the direction of rotation of the fluid/gas mixture. In this manner, one or several mixing 12~9943 steps for the fluid/gas mixture flowin~ in the reaction zonc are produced.
Another embodiment serving to set the fluid~gas mixture in tan~ntial rotary motion is that in which tangentially mounted nozzles ar~ uscd. Irhrouc~h the nozzl~s part of the feed or 2nother fluid, e.g. s-t~am, may be introduced to set the feed proper in rotary rno~ion. ~rhe number of the nozzles is selected according to the need, for instance from2 to 20 nozzles. It is also pos-sible to dispose the feed pipes for the hydrocarbon being cracked entering the reaction zone tangentially in the entrance section of the zone.
According to still another advantageous embodiment, the reaction 20ne has the shape of an outwardly expanding cone over its entire length or in part, for instance only on the part of the supply section. Such a conical shape has the effect of making the distribution of delay time uniform.
It has been established that the appropriate temperature for the cracking reaction is between 410 to 470 degrees and the pressure between 2 and 20 bar. The ratio of the average diameter and the length of the reaction zone is preferably in the range from 1:1 to 1:20.
The invention will now be described in more detail, by way of example only, with reference to the accompanying drawings, in which:-Fig. 1 shows an advantageous embodiment of a methodaccording to the invention as a schematlc process diagram;
Fig. 2 shows an advantageous embodiment of the reactor used in the invention in schematic elevational view;
Fig. 3A shows another advantageous embodiment of the 3~ reactor employed in the process of the invention viewed from above;
Fig. 3B shows the reactor of Fig. 3A in elevational view;
Fig. 4A shows a further advantageous embodiment of the ~99~3 - reactor used in the invention view~d from above; and Fig. 4B shows the reactor of Fig. 4A in elevational view.
In Fig. l, the feed oil is conducted through -the pipe 11 into the furnace 12, wh~re its t~mperature is raised to betw~en ~lO ~r~ 70 d~(3r~es. Irom ~he ~]rnace J2, the oil is conducted t~llOU(j]-l the p;pe 13 into the reactor 14, ~here it flows upward and leaves at the top of the reactor through the pipe 15 to a separate unit (not shown), wherein for insiance gas, petrol, light and heavy fuel oil may be separated from each other. The average delay tiïne in the reaction zone is between 5 and lOO
minutes.
In the embodiment of Fig. 2, a helical member 16 is provided within the reactor 14. The hydrocarbons to be cracked are conducted into the reactor 14 upwards from below, whereby they enter a helical corridor formed by the spiral member 16, and where the actual cracking takes place.
In the embodiment of Fig. 2, the reaction zone 18 may also have two helical members 16 and 17, with opposite directions of the helix. Hereby, the fluid/gas mixture flowing in the reac-tion zone 18 will reverse its rotation.
Figs. 3A and 3B show the lower part of the pressurevessel 14 acting as reaction zone 18, and in which the hydro-carbon flow to be cracked with the lower part of the pressure vessel 14 is introduced upward from below. The nozzles l9 com-municate tangentially through which either part of the feed or another fluid, such as steam for instance, may be introduced in order to set in rotation the hydrocarbon flow that is being cracked.
In the embodiment of Figs. 4A and 4B, on the end of the feed pipe 20 for the hydrocarbons to be cracked, are formed nozzles 21 which force the feed into rotary motion.
Example I:
12~943 On a pilot plant scale, thermal cracking of crude oil was carried out, using a reactor as in Fig. 1, and a similar reactor having no helix system. In other respects, the conditions were equal. The feed oil was the vacuum distilling base of Soviet (ru(le oil. The res~lts are shown in the tab]e attached:-Char~ic~-erislic Feed L'~ er~ics of the base product (Distillltion fr;~ction 180 C+) Without With helix system helix system _____________________________________ ____________________________ Density (g/cm 20 C) 1.0011 1.001 1.002 Asphaltene content t% by weight) 6.28 10.70 11.10 Sulphur content (% by weight) 3.65 3.38 3.54 Viscosity cSt (50 C) 43000 4200 3300 Stability 1) - 2.0 2.1 ____________________~_____________________________________________ 1~ The concept of stability is described in more detail in: van Kerkvoort, ~.J., Nieuwstad) A.J.J. IV: E Congres Intern. du Chauffage Industriel, paper number 220, Paris, 1952.
In ~he the~ïrlal cracking of hydrocarbon oils, heavy oil frlcti~ns are cracked to lighter fractions to increase the yield of the latter. In the cracking process, the Eeed oil is heated in the heating tubes of the cracking furnace to cracking tempera-ture. As a rule, two alternative methods are available. In one of them, cracking takes place in the heating tubes of the crackinq furnace and partly in the pipelines which lead to the process steps following the cracking. In this cracking process the delay times are not exactly known, but they are relatively short, in the order of one minute. The pressure varies greatly, going down from the furnace entrance to the furnace exit. In the other cracking process, the hydrocarbon feed is first heated in the cracking furnace to a suitable reaction temperature, and the actual cracking reaction takes place in a separate reaction zone, where the delay time is considerably lon~er than in the preceding process, that is, in the order of 10 to 30 minutes. No heat is introduced to the reaction zone.
In the last-mentioned process, the reaction zone as a rule consists of an upright, cylindrical pressure vessel, at one end of which the oil feed heated in the cracking furnace is in-troduced and at the other end of which extracted a mixture of liquid and gas to go to further refining steps extracted, for in-stance for distillation. The flow direction in the reaction One has been either downward from above or upward from helow.
In the thermal cracking of hydrocarbon oils, reactions of substantiall~ two kinds take place. One of them is the crack-ing reaction proper, the long-chain molecules being split into smaller molecules, causing reduction of viscosity. The other ., ,j'~l" '~
~Z~9g~3 - reactlon type is called polycondensati~n, whereby the molecules combine and prod~ce pitch and coke as hydrogen is set free. The last-mentioned reaction is an undesired reaction because it re-sults in greater quantities of asphaltelles. Since the condensing reac~ions grow to be signiEicant al hi~ er telllL~(-rat~lres, cn~ea-vours ace made to use lower reactio~ cm~ rt~ Lcs ~nd c~rrc~ )olld-ingly lon~er delay times.
The delay time is very important for thermal cracking.
The cracking has not time to ta~e place if the delay time is too lG short. In a case where the delay time is too long, the cracking products begin to react and to form undesired reaction products.
As a result, an unstable product is formed which causes difficul-ties in the further use of fuel. The aim is therefore to achieve a cracking as uniform as possible. If the flows in the pressure vessel serving as reaction zone are non-uniform, the result will be varying delay times.
In the cracking reaction, light components are formed which evaporate at the temperature and pressure in the reaction zone. Therefore, the density of the liquid/gas mixture decreases as the mixture flows upward in the pressure vessel. Owing to the ~ hydrostatic pressure differential in the pressure vessel, the density of the gas part also decreases as the mixture flows up-ward. The liquid fractions formed in the cracking reactor have a lower density than the feed, which also lowers the density of the liquid/gas mixture. Therefore, the flow velocity is not con-stant in the usually employed cylindrical reactor with uniform thickness, but accelerates as the mixture flows upward.
The thermal cracking procedure disclosed in U~S. Patent No. 4,2~7,387 has a cylindrical vertical pressure vessel serving as reaction zone. With a view to preventing refluxes within the reactor, perforated intermediate plates are provided at the bottom of the reaction zone to form a plurality of mixing sites in the ~09943 reactor. The object is to achievc a delay time as uniform as possible for the fraction fed into the zone. The use of inter-mediate plates has its drawbacks. ~aulty operation of the reac-tor may ca~lse the who]e reactor to be coked to occlusion. The intermeclilte l~lates rnake the co~e removal and reactor cleaning inconvc~ ier~t ~nd e~pensive.
~ n object of the invention is to achieve an in~E~rov~mellt in the processes known in the art. A more ~etailed object of the invention is to provide a process in which a uniform delay time can be attained without the need for intermediate plates that hamper the cleaning process.
According to the present invention there is provided a process for the thermal crac~ing of hydrocarbons, wherein the hydrocarbons are heated to reaction temperature and conducted into a reaction zone as a fluid/gas mixture, where the flow is upwards from below, and wherein the fluid/gas mixture is set in tangential rotation in a pressure vessel defining the reaction zone.
A tangentially rotating, but vertically uniformly up-wards progressing fluid/gas flow with no return flows causing non-uniform delay times is generated in the reaction zone.
The tangentially rotating flow of the fluid/gas mixture can be obtained in a number of ways. In a preferred embodiment, the rotary motion is produced by means of helical members that form a helically ascending corridor in the pressure vessel serv-ing as reactor. In this passage, the f~ow is always in the up-wards direction and no downflows occur. The helix system may extend over the entire length of the reaction zone, or only over part of it. In some instances, it may suffice to restrict the helix system to the entrance section of the reaction zone.
It is also possible to provide in the reactor two or more helix-like members, which reverse the direction of rotation of the fluid/gas mixture. In this manner, one or several mixing 12~9943 steps for the fluid/gas mixture flowin~ in the reaction zonc are produced.
Another embodiment serving to set the fluid~gas mixture in tan~ntial rotary motion is that in which tangentially mounted nozzles ar~ uscd. Irhrouc~h the nozzl~s part of the feed or 2nother fluid, e.g. s-t~am, may be introduced to set the feed proper in rotary rno~ion. ~rhe number of the nozzles is selected according to the need, for instance from2 to 20 nozzles. It is also pos-sible to dispose the feed pipes for the hydrocarbon being cracked entering the reaction zone tangentially in the entrance section of the zone.
According to still another advantageous embodiment, the reaction 20ne has the shape of an outwardly expanding cone over its entire length or in part, for instance only on the part of the supply section. Such a conical shape has the effect of making the distribution of delay time uniform.
It has been established that the appropriate temperature for the cracking reaction is between 410 to 470 degrees and the pressure between 2 and 20 bar. The ratio of the average diameter and the length of the reaction zone is preferably in the range from 1:1 to 1:20.
The invention will now be described in more detail, by way of example only, with reference to the accompanying drawings, in which:-Fig. 1 shows an advantageous embodiment of a methodaccording to the invention as a schematlc process diagram;
Fig. 2 shows an advantageous embodiment of the reactor used in the invention in schematic elevational view;
Fig. 3A shows another advantageous embodiment of the 3~ reactor employed in the process of the invention viewed from above;
Fig. 3B shows the reactor of Fig. 3A in elevational view;
Fig. 4A shows a further advantageous embodiment of the ~99~3 - reactor used in the invention view~d from above; and Fig. 4B shows the reactor of Fig. 4A in elevational view.
In Fig. l, the feed oil is conducted through -the pipe 11 into the furnace 12, wh~re its t~mperature is raised to betw~en ~lO ~r~ 70 d~(3r~es. Irom ~he ~]rnace J2, the oil is conducted t~llOU(j]-l the p;pe 13 into the reactor 14, ~here it flows upward and leaves at the top of the reactor through the pipe 15 to a separate unit (not shown), wherein for insiance gas, petrol, light and heavy fuel oil may be separated from each other. The average delay tiïne in the reaction zone is between 5 and lOO
minutes.
In the embodiment of Fig. 2, a helical member 16 is provided within the reactor 14. The hydrocarbons to be cracked are conducted into the reactor 14 upwards from below, whereby they enter a helical corridor formed by the spiral member 16, and where the actual cracking takes place.
In the embodiment of Fig. 2, the reaction zone 18 may also have two helical members 16 and 17, with opposite directions of the helix. Hereby, the fluid/gas mixture flowing in the reac-tion zone 18 will reverse its rotation.
Figs. 3A and 3B show the lower part of the pressurevessel 14 acting as reaction zone 18, and in which the hydro-carbon flow to be cracked with the lower part of the pressure vessel 14 is introduced upward from below. The nozzles l9 com-municate tangentially through which either part of the feed or another fluid, such as steam for instance, may be introduced in order to set in rotation the hydrocarbon flow that is being cracked.
In the embodiment of Figs. 4A and 4B, on the end of the feed pipe 20 for the hydrocarbons to be cracked, are formed nozzles 21 which force the feed into rotary motion.
Example I:
12~943 On a pilot plant scale, thermal cracking of crude oil was carried out, using a reactor as in Fig. 1, and a similar reactor having no helix system. In other respects, the conditions were equal. The feed oil was the vacuum distilling base of Soviet (ru(le oil. The res~lts are shown in the tab]e attached:-Char~ic~-erislic Feed L'~ er~ics of the base product (Distillltion fr;~ction 180 C+) Without With helix system helix system _____________________________________ ____________________________ Density (g/cm 20 C) 1.0011 1.001 1.002 Asphaltene content t% by weight) 6.28 10.70 11.10 Sulphur content (% by weight) 3.65 3.38 3.54 Viscosity cSt (50 C) 43000 4200 3300 Stability 1) - 2.0 2.1 ____________________~_____________________________________________ 1~ The concept of stability is described in more detail in: van Kerkvoort, ~.J., Nieuwstad) A.J.J. IV: E Congres Intern. du Chauffage Industriel, paper number 220, Paris, 1952.
2~
Claims (21)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for the thermal cracking of hydrocarbons, wherein the hydrocarbons are heated to reaction temperature and conducted into a reaction zone as a fluid/gas mixture, where the flow is upwards from below, and wherein the fluid/gas mixture is set in tangential rotation in a pressure vessel defining the reaction zone.
2. A process according to claim 1, wherein the fluid/
gas mixture is set in rotation with the aid of at least one helix-like member.
gas mixture is set in rotation with the aid of at least one helix-like member.
3. A process according to claim 2, wherein the helix-like member is disposed over the entire length of the pressure vessel.
4. A process according to claim 2, wherein the helix-like member is disposed over part of the length of the pressure vessel, or merely at the entrance section and/or the exit section.
5. A process according to claim 1, 2 or 3, wherein the helix-like member comprises two or more helix systems which can reverse the rotation of the fluid/gas mixture.
6. A process according to claim 1, wherein the fluid/
gas mixture is set in rotation with the aid of nozzles.
gas mixture is set in rotation with the aid of nozzles.
7. A process according to claim 6, wherein the nozzles communicate tangentially with the entrance section of the reaction zone.
8. A process according to claim 6 or 7, wherein the nozzles are in the reaction zone on the extension of the feed pipe for the hydrocarbons.
9. A process according to claim 6 or 7, wherein the fluid/gas mixture is set in rotation with the aid of a nozzle system, through which part of the supply, or steam or another fluid, is conducted into the pressure vessel.
10. A process according to claim 1, 2 or 3, wherein the thermal cracking is accomplished in the reaction zone at a tem-perature of 410 to 470 degrees, under pressure 2 to 20 bar, and with an average delay time between 5 and 100 minutes.
11. A process according to claim l, 2 or 3, wherein the pressure vessel is an upwardly expanding conical pressure vessel.
12. An apparatus for the thermal cracking of hydrocar-bons, comprising a pressure vessel defining a reaction zone where-in the flow is upwards from below, and means for setting a fluid/
gas mixture in the pressure vessel in tangential rotation.
gas mixture in the pressure vessel in tangential rotation.
13. An apparatus according to claim 12, wherein said setting means comprise a helix-like member.
14. An apparatus according to claim 13, wherein the helix-like member is disposed over the entire length of the pres-sure vessel.
15. An apparatus according to claim 13, wherein the helix-like member is disposed over part of the length of the pres-sure vessel, or merely at the entrance section and/or the exit section.
16. An apparatus according to claim 13, wherein the helix-like member comprises two or more helix systems which can reverse the rotation of the fluid/gas mixture.
17. An apparatus according to claim 12, wherein said setting means comprise nozzles.
18. An apparatus according to claim 12, wherein the nozzles communicate tangentially with the entrance section of the reaction zone.
19. An apparatus acording to claim 12, wherein the nozzles are in the reaction zone on the extension of the feed pipe for the hydrocarbons.
20. An apparatus according to claim 12, wherein the setting means comprises a nozzle system, through which part of the supply, or steam, or another fluid is introduced into the pressure vessel.
21. An apparatus according to claim 12, wherein the pressure vessel is an upwardly expanding conical pressure vessel.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI822119A FI65274C (en) | 1982-06-14 | 1982-06-14 | FOERFARANDE FOER TERMISK KRACKNING AV KOLVAETEOLJA |
| FI822119 | 1982-06-14 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1209943A true CA1209943A (en) | 1986-08-19 |
Family
ID=8515691
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000429300A Expired CA1209943A (en) | 1982-06-14 | 1983-05-31 | Procedure for thermal cracking of hydrocarbon oils |
Country Status (13)
| Country | Link |
|---|---|
| JP (1) | JPS59501068A (en) |
| BE (1) | BE896901A (en) |
| CA (1) | CA1209943A (en) |
| CS (1) | CS241059B2 (en) |
| DE (1) | DE3390051T1 (en) |
| FI (1) | FI65274C (en) |
| FR (1) | FR2528444B1 (en) |
| GB (1) | GB2133034B (en) |
| HU (1) | HU202573B (en) |
| IE (1) | IE55266B1 (en) |
| IT (1) | IT1163501B (en) |
| NL (1) | NL8320167A (en) |
| WO (1) | WO1984000035A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8262903B2 (en) | 2006-09-28 | 2012-09-11 | Chiyoda Corporation | Process, reactor and facility for thermally cracking heavy petroleum oil |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0232772B1 (en) * | 1986-02-05 | 1989-12-27 | Siemens Aktiengesellschaft | Process for preparing a pulverulent amorphous material by way of a milling process |
| FI85598C (en) * | 1989-09-13 | 1992-05-11 | Antero Ollila | FOERFARANDE OCH ANORDNING FOER TERMISK KRACKNING AV KOLVAETEOLJOR OCH FOER ANDRA VAETSKE / -GASREAKTIONER. |
| LT3884B (en) | 1994-06-22 | 1996-04-25 | Akcine Bendrove Mazeikiu Nafta | Reactor of thermal cracking |
| FR2741889B1 (en) * | 1995-12-04 | 1999-01-29 | Total Raffinage Distribution | IMPROVEMENTS IN PROCESSES AND DEVICES FOR VISCOREDUCING HEAVY HYDROCARBON LOADS |
| AU2004241092B2 (en) | 2003-05-15 | 2009-06-04 | Covidien Ag | Tissue sealer with non-conductive variable stop members and method of sealing tissue |
| JP5038674B2 (en) | 2006-09-28 | 2012-10-03 | 千代田化工建設株式会社 | Pyrolysis treatment method and pyrolysis treatment equipment for heavy petroleum oil |
| US8512371B2 (en) | 2009-10-06 | 2013-08-20 | Covidien Lp | Jaw, blade and gap manufacturing for surgical instruments with small jaws |
| US8852186B2 (en) | 2011-08-09 | 2014-10-07 | Covidien Lp | Microwave sensing for tissue sealing |
| US8864795B2 (en) | 2011-10-03 | 2014-10-21 | Covidien Lp | Surgical forceps |
| US8968308B2 (en) | 2011-10-20 | 2015-03-03 | Covidien Lp | Multi-circuit seal plates |
| US9713493B2 (en) | 2012-04-30 | 2017-07-25 | Covidien Lp | Method of switching energy modality on a cordless RF device |
| US9713491B2 (en) | 2013-02-19 | 2017-07-25 | Covidien Lp | Method for manufacturing an electrode assembly configured for use with an electrosurigcal instrument |
| US9717548B2 (en) | 2013-09-24 | 2017-08-01 | Covidien Lp | Electrode for use in a bipolar electrosurgical instrument |
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| DE27692C (en) * | G. SCHRADßR in Ehrenfeld, Venloerstr. 168 | Automatic protective device fMT joining and dressing machines | ||
| GB178734A (en) * | 1921-05-09 | 1922-04-27 | Frederick Southwell Cripps | Improvements in apparatus for evaporating paraffin or other liquids, and mixing the vapours produced with coal gas |
| DE749498C (en) * | 1942-05-29 | 1944-11-24 | Standing cracking and distillation kettle with feed nozzles for hot flame gases and atomized oil | |
| US2460463A (en) * | 1946-11-07 | 1949-02-01 | Phillips Petroleum Co | Process for the noncatalytic cracking of a hydrocarbon oil |
| US2717865A (en) * | 1951-05-17 | 1955-09-13 | Exxon Research Engineering Co | Coking of heavy hydrocarbonaceous residues |
| US2759880A (en) * | 1951-10-31 | 1956-08-21 | Exxon Research Engineering Co | Short-time contacting of fluids with solids in hydrocarbon conversion |
| US3498753A (en) * | 1966-07-04 | 1970-03-03 | Nippon Zeon Co | Apparatus for thermal cracking of hydrocarbon |
| US3652451A (en) * | 1968-12-20 | 1972-03-28 | Universal Oil Prod Co | Fluid distribution for fluid-solids contacting chambers |
| FR2229757A1 (en) * | 1973-05-14 | 1974-12-13 | Union Carbide Corp | Hydrocarbon cracker using hot gases - for naphtha, gas oil or crude feedstock |
| DE2645649C2 (en) * | 1975-10-14 | 1982-09-02 | Chiyoda Chemical Engineering & Construction Co. Ltd., Yokohama, Kanagawa | Process for the thermal cracking of heavy hydrocarbons |
| JPS5247006A (en) * | 1975-10-14 | 1977-04-14 | Kureha Chem Ind Co Ltd | Method for preventing deposition of coke to vessels for thermal cracki ng of heavy hydrocarbons |
| JPS5247007A (en) * | 1975-10-14 | 1977-04-14 | Kureha Chem Ind Co Ltd | Method and apparatus for preventing deposition of coke to vessels for thermal cracking of heavy hydrocarbons |
| CA1137434A (en) * | 1978-07-11 | 1982-12-14 | Mohammed Akbar | Process for the continuous thermal cracking of hydrocarbon oils |
| EP0027692B1 (en) * | 1979-10-18 | 1984-05-30 | Imperial Chemical Industries Plc | A process and reactor for the pyrolysis of a hydrocarbon feedstock |
-
1982
- 1982-06-14 FI FI822119A patent/FI65274C/en not_active IP Right Cessation
-
1983
- 1983-05-31 CA CA000429300A patent/CA1209943A/en not_active Expired
- 1983-05-31 BE BE0/210892A patent/BE896901A/en not_active IP Right Cessation
- 1983-06-10 GB GB08401584A patent/GB2133034B/en not_active Expired
- 1983-06-10 IT IT21574/83A patent/IT1163501B/en active
- 1983-06-10 NL NL8320167A patent/NL8320167A/en unknown
- 1983-06-10 HU HU832320A patent/HU202573B/en not_active IP Right Cessation
- 1983-06-10 DE DE19833390051 patent/DE3390051T1/en not_active Ceased
- 1983-06-10 WO PCT/FI1983/000044 patent/WO1984000035A1/en active Application Filing
- 1983-06-10 JP JP58501848A patent/JPS59501068A/en active Granted
- 1983-06-13 IE IE1379/83A patent/IE55266B1/en unknown
- 1983-06-13 CS CS834231A patent/CS241059B2/en unknown
- 1983-06-14 FR FR8309824A patent/FR2528444B1/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8262903B2 (en) | 2006-09-28 | 2012-09-11 | Chiyoda Corporation | Process, reactor and facility for thermally cracking heavy petroleum oil |
Also Published As
| Publication number | Publication date |
|---|---|
| IT8321574A0 (en) | 1983-06-10 |
| WO1984000035A1 (en) | 1984-01-05 |
| JPS59501068A (en) | 1984-06-21 |
| IE831379L (en) | 1983-12-14 |
| FI65274C (en) | 1984-04-10 |
| DE3390051T1 (en) | 1984-06-14 |
| HUT34535A (en) | 1985-03-28 |
| NL8320167A (en) | 1984-04-02 |
| GB8401584D0 (en) | 1984-02-22 |
| IE55266B1 (en) | 1990-07-18 |
| FI65274B (en) | 1983-12-30 |
| BE896901A (en) | 1983-09-16 |
| HU202573B (en) | 1991-03-28 |
| FR2528444A1 (en) | 1983-12-16 |
| FI822119A0 (en) | 1982-06-14 |
| CS423183A2 (en) | 1985-07-16 |
| CS241059B2 (en) | 1986-03-13 |
| IT1163501B (en) | 1987-04-08 |
| GB2133034B (en) | 1986-05-29 |
| FR2528444B1 (en) | 1987-06-19 |
| JPS6362557B2 (en) | 1988-12-02 |
| GB2133034A (en) | 1984-07-18 |
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