CA1112198A - Process for cracking heavy liquid hydrocarbons - Google Patents
Process for cracking heavy liquid hydrocarbonsInfo
- Publication number
- CA1112198A CA1112198A CA318,899A CA318899A CA1112198A CA 1112198 A CA1112198 A CA 1112198A CA 318899 A CA318899 A CA 318899A CA 1112198 A CA1112198 A CA 1112198A
- Authority
- CA
- Canada
- Prior art keywords
- molten salt
- weight
- amount
- heavy liquid
- cracking
- 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
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
- C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
Abstract
TITLE OF THE INVENTION
Process for Cracking Heavy Liquid hydrocarbons ABSTRACT OF THE DISCLOSURE
Heavy liquid hydrocarbons containing carbon residue are cracked (A) in the presence of a molten salt of a member selected from the group consisting of basic compounds of alkali metals, alkaline earth metals and mixtures thereof, (B) at least a part of the molten salt being used in a form of mist, (C) the amount of the molten salt being more than 1 part by weight, but not more than 10 parts by weight per 1 part by weight of the heavy liquid hydrocarbons, (D) the amount of the carbon residue being not more than 0.03 parts by weight per 1 part by weight of the molten salt, and (E) amount of steam, reaction time, reaction temperature and amount of the molten salt being controlled so as to render the weight ratio of carbon after cracking to the molten salt not more than 0.002.
Process for Cracking Heavy Liquid hydrocarbons ABSTRACT OF THE DISCLOSURE
Heavy liquid hydrocarbons containing carbon residue are cracked (A) in the presence of a molten salt of a member selected from the group consisting of basic compounds of alkali metals, alkaline earth metals and mixtures thereof, (B) at least a part of the molten salt being used in a form of mist, (C) the amount of the molten salt being more than 1 part by weight, but not more than 10 parts by weight per 1 part by weight of the heavy liquid hydrocarbons, (D) the amount of the carbon residue being not more than 0.03 parts by weight per 1 part by weight of the molten salt, and (E) amount of steam, reaction time, reaction temperature and amount of the molten salt being controlled so as to render the weight ratio of carbon after cracking to the molten salt not more than 0.002.
Description
BACKGROUND OF THE INVENTION
Field of the Invention This invention relates to a process for cracking heavy liquid hydrocarbons containing carbon residue.
~escription of the Prior Act The present inventors previously proposed a process for cracking hydrocarbons in Japanese Patent Application No.
97679/1976. This process is suitable for cracking heavy liquid hydrocarbons and the feature is that a mist of a member selected from the group consisting of basic compounds of alkali metals, alkaline earth metals and mixtures thereof is used and the amount of the molten salt is 0.01 - 1 part by weight per 1 part by weight of the hydrocarbon.
However, it has been found that a mixture of the molten salt and the carbon residue becomes viscous and is apt to attach to the wall of the cracking reactor and sometimes the inlet of the hydrocarbon feed is clogged when the amount of the molten salt is small and the molten salt and the heavy liquid hydrocarbon are mixed at a low temperature and steam is not fed in a large amount upon cracking the heavy liquid hydrocarbon containing a large amount of carbon residue.
From a commercial point of view, it is desirable to lessen the amount of steam as far as possible, and a very high temperature of the molten salt is not desirable from a view-point of apparatus materials. Further, heavy liquid hydrocarbons should not be pre-heated over a certain temperature so as to prevent the heat decomposition before feeding to a ', X
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1 ~¦ cxacking reactor. In addition it is desirable that the molten
Field of the Invention This invention relates to a process for cracking heavy liquid hydrocarbons containing carbon residue.
~escription of the Prior Act The present inventors previously proposed a process for cracking hydrocarbons in Japanese Patent Application No.
97679/1976. This process is suitable for cracking heavy liquid hydrocarbons and the feature is that a mist of a member selected from the group consisting of basic compounds of alkali metals, alkaline earth metals and mixtures thereof is used and the amount of the molten salt is 0.01 - 1 part by weight per 1 part by weight of the hydrocarbon.
However, it has been found that a mixture of the molten salt and the carbon residue becomes viscous and is apt to attach to the wall of the cracking reactor and sometimes the inlet of the hydrocarbon feed is clogged when the amount of the molten salt is small and the molten salt and the heavy liquid hydrocarbon are mixed at a low temperature and steam is not fed in a large amount upon cracking the heavy liquid hydrocarbon containing a large amount of carbon residue.
From a commercial point of view, it is desirable to lessen the amount of steam as far as possible, and a very high temperature of the molten salt is not desirable from a view-point of apparatus materials. Further, heavy liquid hydrocarbons should not be pre-heated over a certain temperature so as to prevent the heat decomposition before feeding to a ', X
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1 ~¦ cxacking reactor. In addition it is desirable that the molten
2 ¦ I salt can be recirculated without any regeneration procedure.
3 ¦~ It has been demanded to develop a process which can
4 1l satisfy the above mentioned conditions and does not suffer 1 from the above-mentioned drawbacks upon cracking heavy oils 6 containing much carbon residue.
g An object of the present invention is to provide a process for cracking hydrocarbons which is free from clogging 11 near the feed inlet of heavy liauid hydrocarbons.
12 Another object of the present invention is to provide 13 a process for cracking hydrocarbons in which steam consumption 14 is very little.
A further object of the present invention is to provide 16 a process for cracking hydrocarbons which utilizes remarkably 17 reduced quantities of circulating molten salt.
18 Still another object of the present invention is to provide a process for cracking hydrocarbons in which a molten salt can be reused without treatment for decreasing carbon.
21 A still further object of the present invention is 22 to provide a process for cracking hydrocarbons in which carbon , -23 is eliminated by the water gas reaction with steam.
24 Still another object of the present invention is to provide a process for cracking hydrocarbons which utilizes 26 only a small quantity of heat and can be conducted in a compact 27 apparatus.
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A still further object of the present invention is to provide a process for cracking hydrocarbons which uses only a small amount of a heat transfer medium and is free from danger of fire.
Still another object of the present invention is to - provide a process for cracking hydrocarbons which is free from deposition of carbon and tar-like material in the heat de-' composition device and the quenching device.
According to the present invention, there is provided a process which comprises cracking heavy liquid hydrocarbons containing carbon residue, (A) in the presence of a molten salt of a member selected from the group consisting of basic compounds of alkali metals, alkaline earth metals and mixtures thereof, (B) at least a part of the molten salt being used in a form of mist having an average particle size not greater than 300 microns, (C) the amount of the molten salt being more than 1 part by weight, but not more than 10 parts by weight per 1 part by weight of the heavy liquid hydrocarbons, (D) the amount of the carbon residue being not more than : 0.03 parts by weight per 1 part by weight of the molten salt, and (E) amount of steam, reaction time, reaction temperature and amount of the molten salt being controlled so as to render the weight ratio of carbon after cracking to the molten salt not more than 0.002.
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1 ~! BRIEF DESCRIPTION OF THE DRAWING
2 ll The drawing shows diagrammatically apparatus which 3 ll may be used for carrying out the present invention.
g An object of the present invention is to provide a process for cracking hydrocarbons which is free from clogging 11 near the feed inlet of heavy liauid hydrocarbons.
12 Another object of the present invention is to provide 13 a process for cracking hydrocarbons in which steam consumption 14 is very little.
A further object of the present invention is to provide 16 a process for cracking hydrocarbons which utilizes remarkably 17 reduced quantities of circulating molten salt.
18 Still another object of the present invention is to provide a process for cracking hydrocarbons in which a molten salt can be reused without treatment for decreasing carbon.
21 A still further object of the present invention is 22 to provide a process for cracking hydrocarbons in which carbon , -23 is eliminated by the water gas reaction with steam.
24 Still another object of the present invention is to provide a process for cracking hydrocarbons which utilizes 26 only a small quantity of heat and can be conducted in a compact 27 apparatus.
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A still further object of the present invention is to provide a process for cracking hydrocarbons which uses only a small amount of a heat transfer medium and is free from danger of fire.
Still another object of the present invention is to - provide a process for cracking hydrocarbons which is free from deposition of carbon and tar-like material in the heat de-' composition device and the quenching device.
According to the present invention, there is provided a process which comprises cracking heavy liquid hydrocarbons containing carbon residue, (A) in the presence of a molten salt of a member selected from the group consisting of basic compounds of alkali metals, alkaline earth metals and mixtures thereof, (B) at least a part of the molten salt being used in a form of mist having an average particle size not greater than 300 microns, (C) the amount of the molten salt being more than 1 part by weight, but not more than 10 parts by weight per 1 part by weight of the heavy liquid hydrocarbons, (D) the amount of the carbon residue being not more than : 0.03 parts by weight per 1 part by weight of the molten salt, and (E) amount of steam, reaction time, reaction temperature and amount of the molten salt being controlled so as to render the weight ratio of carbon after cracking to the molten salt not more than 0.002.
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1 ~! BRIEF DESCRIPTION OF THE DRAWING
2 ll The drawing shows diagrammatically apparatus which 3 ll may be used for carrying out the present invention.
5 1I DESCRIPTION OF THE PREFERRED EMBODIMENT
6 l~ The representative heavy liquid hydrocarbons used in
7 1I the present invention are crude oil, heavy oil, light oil
8 ¦I from low pressure distillation, bottom residue from low pressure distillation and the like. These heavy liquid hydrocarbons contain carbon residue such as asphaltene, resins, high polymer 11 compounds and the like which become carbon upon heating.
12 Clogging at the feed inlet of the heavy liauid 13 hydrocarbon occurs when viscosity of the mixture of the heavy 14 liquid hydrocarbon and the molten salt is remarkably high.
Therefore, it is necessary to lower the viscosity for the 16 purpose of preventing clogging at the feed inlet. Thus the 17 amount of the carbon residue (Conradson carbon) is not more 18 than 0.03 parts by weight per 1 part by weight of the molten 19 salt, preferably 0.005 - 0.020 parts by weight per 1 part by weight of the molten salt.
- 21 When the amount of carbon residue in the heavv liquid22 hydrocarbon per the molten salt is larger than the upper limit, 23 a mixture of the molten salt and the carbon residue is apt to 24 attach to the cracking reactor wall. On the contrary, when the amount is too small, the amount of the molten salt is 26 ¦ unnecessarily large so that such procedure is not economical.
27 When the temperature of the mixture is lowered, the , il .
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il viscosity increases rapidly. Therefore, the amount of the 2 I molten salt is more than 1 part by weight, but not more than 3 1l 10 parts by weight, preferably not more than 5 parts by weight 4 ll per one part by weight of the heavy liquid hydrocarbon. At a 5 1 ¦ region over the upper limit the viscosity of the mixture does I not remarkably decrease and it is not desirable to use such 7 a large amount of molten salt from an economical point of view.
On the contrary, at a region below the lower limit, a mixture
12 Clogging at the feed inlet of the heavy liauid 13 hydrocarbon occurs when viscosity of the mixture of the heavy 14 liquid hydrocarbon and the molten salt is remarkably high.
Therefore, it is necessary to lower the viscosity for the 16 purpose of preventing clogging at the feed inlet. Thus the 17 amount of the carbon residue (Conradson carbon) is not more 18 than 0.03 parts by weight per 1 part by weight of the molten 19 salt, preferably 0.005 - 0.020 parts by weight per 1 part by weight of the molten salt.
- 21 When the amount of carbon residue in the heavv liquid22 hydrocarbon per the molten salt is larger than the upper limit, 23 a mixture of the molten salt and the carbon residue is apt to 24 attach to the cracking reactor wall. On the contrary, when the amount is too small, the amount of the molten salt is 26 ¦ unnecessarily large so that such procedure is not economical.
27 When the temperature of the mixture is lowered, the , il .
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il viscosity increases rapidly. Therefore, the amount of the 2 I molten salt is more than 1 part by weight, but not more than 3 1l 10 parts by weight, preferably not more than 5 parts by weight 4 ll per one part by weight of the heavy liquid hydrocarbon. At a 5 1 ¦ region over the upper limit the viscosity of the mixture does I not remarkably decrease and it is not desirable to use such 7 a large amount of molten salt from an economical point of view.
On the contrary, at a region below the lower limit, a mixture
9 I of the molten salt and the carbon residue hecomes viscous and is apt to attach to a wall of a cracking reactor and sometimes 11 the feed inlet of the heavy liquid hydrocarbon is clogged where 12 steam is not present in a large amount.
13 A molten salt is preferable which serves to lessen 14 the carbon (produced in the cracking reactor) by water gas reaction as far,as possible. Therefore, according to the present 16 invention, as the molten salt there is used a member from the 17 group consisting of basic compounds of alkali metals, alkaline 18 earth metals and mixtures thereof. In order to avoid that a mixture of the molten salt and the carbon residue becomes viscous to clog the inlet of the heavy liquid hydrocarbon, a 21 molten salt having melting point of not higher than 450C is 22 preferable, and in particular, that having melting point of 23 not higher than 400C is more preferable. For example, a 24 mixture of Li2CO3(mp. 618C), Na2CO3(mp. 851C) and K2CO3 (mp. 891C), preferably, an equimolar mixture thereof (the 26 eutectic point is 385C), is used. A part of these compounds 27 may be the sulfide or sulfite.
' 1 ~ For the purpose of effecting water gas reaction in the 2 ~ cracking reaction, steam is present in the reaction system. The 3 I amount of steam is not critical. However, it is not economical 4 I to use in a large amount, but where the amount is too small, the S I water gas reaction can not occur sufficiently. In general, the 6 weight ratio of steam to the heavy liquid hydrocarbon is 0.5 - 5.0~ - -I preferably 0.5 - 2Ø
8 ~ At least a part of the~olten salt is used in a form of ¦ mist and thereby even a small amount of molten salt can intimately !
I contact with the heavy liauid hydrocarbon to proceed smoothly the 11 water gas reaction. The average particle size of the molten salt 12 is usually not larger than 300 microns, preferably not larger 13 than 100 microns.
14 The molten salt mist may be easily produced by using a venturi nozzle and passing steam.
16 Other method for producing the mist may be the use of a 17 pressure nozzle such as single hole nozzle, collision spray 18 valve, spiral spray valve, and the like; the method of rotation 19 ¦ such as rotating disk, rotating pan, rotating spray and the ¦ like; the method of gas-atomizing spray such as air or gas-21 atomising nozzle and the like, and a vibration method.
22 , Further, the mist may be obtained by dissolving or 23 ~ suspending the salt in a heavy liquid hydrocarbon or water used 24 1¦ as a diluting vapor and supplying the resulting solution or ' suspension to the cracking apparatus.
26 ' Among these methods for producing mist, a method where 27 ~ at least a part of the molten salt is made into mist before the 28 molten salt is mixed with the heavy liquid hydrocarbon is preferred.
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~121~8 The process of the present invention is particularly 2 l, effective when used for cracking of an external heating type.
3 I Naturally the process of the present invention can be applied 4 `~ to cracking of an internal heating type, but in case of cracking 1l of an internal heating type, a large amount of high temperature 6 ¦ gas for heating is used so that the above-mentioned partial 7 ¦I cooling of the molten salt can be avoided to some extent and therefore the process of Japanese Patent Application No. 97679/1976 may be used in cracking of an internal heating type.
The cracking is usually carried out at 600 - 900C, 11 preferably 700 - 850C and for 0.001 - 2 seconds, preferably, 12 0.005 - 1.0 second, and more preferably, 0.01 - 0.3 seconds.
13 The reaction conditions such as amount of steam, 14 reaction time, reaction temperature and amount of the molten salt are controlled so as to render the weight ratio of carbon 16 discharged from the cracking reactor to the molten salt not 17 more than 0.002, preferably not more than 0.001. Thus the molten 18 salt can be reused without subjec.ted to a regeneration treatment.
19 Where carbon amount is large after completion of the reaction, there occurs foaming of the molten salt so that the 21 separation from the decomposition gas can not be smoothly 22 effected.
23 Quenching the reaction mixtures discharged from the 24 cracking reactor is preferable to prevent side reactions. The reaction mixture is quenched to a temperature at which the 26 I molten salt does not solidifies. It is usually, for example, 27 1l 400 - 600C though it depends on each molten salt. After ~1 - 8 -1 1l ' i, Il i quenched, the molten salt is separated and recirculated, and 2 ~I the cracked gas may be separated into each component and ¦ purified in accordance with methods as used in usual ethylene 4 1` ¦ production plants.
S I EXAMPLES 1 - 3 and CO~ARATIVE EXAMPLES l - 3 Referring to the drawing, steam 1 superheated to 750C
7 ~ by a heater 2 was introduced into a venturi throat 7. The 8 venturi throat portion was provided with a small lateral bore 9 having a diameter of 2 mm. Through the small lateral bore was supplied an equimolar mixture of Na2CO3-K2CO3-Li2CO3 kept 11 at 750C as a molten salt to produce a mist of the molten salt.
12 A mixture of Minas crude oil 3 (Conradson carbon 13 residue : 2.5% by weight) and steam 5 (10% of total steam feed) 14 was fed at 300C to an upper portion 9 of a reactor pipe 10 (21.7 mm. of outer diameter and 14.3 mm. of inner diameter and 16 11 m. in length) of an external heating type disposed below 17 the ventur1 throat and heated by a heater 11 to effect cracking.
18 The Minas crude oil 3 and steam 5 were heated by 19 heaters 4 and 6, respectively. After cracking, the reaction mixture was quenched at a quenching portion 12 to 500C and 21 then the molten salt and the cracked gas were separated at 22 separator 13. The cracked gas 17 thus separated was sent to a 23 purification step and the molten salt thus separated was 24 collected in a drum 14, transferred by a pump 15 driven by a motor M and heated by a heater 16 for reuse.
26 The reaction conditions and reaction results are 27 shown in Table 1 below.
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13 A molten salt is preferable which serves to lessen 14 the carbon (produced in the cracking reactor) by water gas reaction as far,as possible. Therefore, according to the present 16 invention, as the molten salt there is used a member from the 17 group consisting of basic compounds of alkali metals, alkaline 18 earth metals and mixtures thereof. In order to avoid that a mixture of the molten salt and the carbon residue becomes viscous to clog the inlet of the heavy liquid hydrocarbon, a 21 molten salt having melting point of not higher than 450C is 22 preferable, and in particular, that having melting point of 23 not higher than 400C is more preferable. For example, a 24 mixture of Li2CO3(mp. 618C), Na2CO3(mp. 851C) and K2CO3 (mp. 891C), preferably, an equimolar mixture thereof (the 26 eutectic point is 385C), is used. A part of these compounds 27 may be the sulfide or sulfite.
' 1 ~ For the purpose of effecting water gas reaction in the 2 ~ cracking reaction, steam is present in the reaction system. The 3 I amount of steam is not critical. However, it is not economical 4 I to use in a large amount, but where the amount is too small, the S I water gas reaction can not occur sufficiently. In general, the 6 weight ratio of steam to the heavy liquid hydrocarbon is 0.5 - 5.0~ - -I preferably 0.5 - 2Ø
8 ~ At least a part of the~olten salt is used in a form of ¦ mist and thereby even a small amount of molten salt can intimately !
I contact with the heavy liauid hydrocarbon to proceed smoothly the 11 water gas reaction. The average particle size of the molten salt 12 is usually not larger than 300 microns, preferably not larger 13 than 100 microns.
14 The molten salt mist may be easily produced by using a venturi nozzle and passing steam.
16 Other method for producing the mist may be the use of a 17 pressure nozzle such as single hole nozzle, collision spray 18 valve, spiral spray valve, and the like; the method of rotation 19 ¦ such as rotating disk, rotating pan, rotating spray and the ¦ like; the method of gas-atomizing spray such as air or gas-21 atomising nozzle and the like, and a vibration method.
22 , Further, the mist may be obtained by dissolving or 23 ~ suspending the salt in a heavy liquid hydrocarbon or water used 24 1¦ as a diluting vapor and supplying the resulting solution or ' suspension to the cracking apparatus.
26 ' Among these methods for producing mist, a method where 27 ~ at least a part of the molten salt is made into mist before the 28 molten salt is mixed with the heavy liquid hydrocarbon is preferred.
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~121~8 The process of the present invention is particularly 2 l, effective when used for cracking of an external heating type.
3 I Naturally the process of the present invention can be applied 4 `~ to cracking of an internal heating type, but in case of cracking 1l of an internal heating type, a large amount of high temperature 6 ¦ gas for heating is used so that the above-mentioned partial 7 ¦I cooling of the molten salt can be avoided to some extent and therefore the process of Japanese Patent Application No. 97679/1976 may be used in cracking of an internal heating type.
The cracking is usually carried out at 600 - 900C, 11 preferably 700 - 850C and for 0.001 - 2 seconds, preferably, 12 0.005 - 1.0 second, and more preferably, 0.01 - 0.3 seconds.
13 The reaction conditions such as amount of steam, 14 reaction time, reaction temperature and amount of the molten salt are controlled so as to render the weight ratio of carbon 16 discharged from the cracking reactor to the molten salt not 17 more than 0.002, preferably not more than 0.001. Thus the molten 18 salt can be reused without subjec.ted to a regeneration treatment.
19 Where carbon amount is large after completion of the reaction, there occurs foaming of the molten salt so that the 21 separation from the decomposition gas can not be smoothly 22 effected.
23 Quenching the reaction mixtures discharged from the 24 cracking reactor is preferable to prevent side reactions. The reaction mixture is quenched to a temperature at which the 26 I molten salt does not solidifies. It is usually, for example, 27 1l 400 - 600C though it depends on each molten salt. After ~1 - 8 -1 1l ' i, Il i quenched, the molten salt is separated and recirculated, and 2 ~I the cracked gas may be separated into each component and ¦ purified in accordance with methods as used in usual ethylene 4 1` ¦ production plants.
S I EXAMPLES 1 - 3 and CO~ARATIVE EXAMPLES l - 3 Referring to the drawing, steam 1 superheated to 750C
7 ~ by a heater 2 was introduced into a venturi throat 7. The 8 venturi throat portion was provided with a small lateral bore 9 having a diameter of 2 mm. Through the small lateral bore was supplied an equimolar mixture of Na2CO3-K2CO3-Li2CO3 kept 11 at 750C as a molten salt to produce a mist of the molten salt.
12 A mixture of Minas crude oil 3 (Conradson carbon 13 residue : 2.5% by weight) and steam 5 (10% of total steam feed) 14 was fed at 300C to an upper portion 9 of a reactor pipe 10 (21.7 mm. of outer diameter and 14.3 mm. of inner diameter and 16 11 m. in length) of an external heating type disposed below 17 the ventur1 throat and heated by a heater 11 to effect cracking.
18 The Minas crude oil 3 and steam 5 were heated by 19 heaters 4 and 6, respectively. After cracking, the reaction mixture was quenched at a quenching portion 12 to 500C and 21 then the molten salt and the cracked gas were separated at 22 separator 13. The cracked gas 17 thus separated was sent to a 23 purification step and the molten salt thus separated was 24 collected in a drum 14, transferred by a pump 15 driven by a motor M and heated by a heater 16 for reuse.
26 The reaction conditions and reaction results are 27 shown in Table 1 below.
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Claims (5)
OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process which comprises cracking heavy liquid hydrocarbons containing carbon residue, (A) in the presence of a molten salt of a member selected from the group consisting of basic compounds of alkali metals, alkaline earth metals and mixtures thereof, (B) at least a part of the molten salt being used in a form of mist having an average particle size not greater than 300 microns, (C) the amount of the molten salt being more than 1 part by weight, but not more than 10 parts by weight per 1 part by weight of the heavy liquid hydrocarbons, (D) the amount of the carbon residue being not more than 0.03 parts by weight per 1 part by weight of the molten salt, and (E) amount of steam, reaction time, reaction temperature and amount of the molten salt being controlled so as to render the weight ratio of carbon after cracking to the molten salt not more than 0.002.
2. A process according to claim 1 in which the molten salt is a mixture of lithium carbonate, sodium carbonate and potassium carbonate.
3. A process according to claim 1 or 2 in which at least a part of the molten salt is made into mist before the molten salt is mixed with the heavy liquid hydrocarbons.
4. A process according to claim 1 in which the amount of steam is 0.5 - 5.0 parts by weight per 1 part by weight of the heavy liquid hydrocarbons, the reaction time is 0.001 - 2 seconds and the reaction temperature is 600 - 900°C.
5. A process according to claim 1 in which the average particle size of the molten salt in the mist is not larger than 100 microns.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1412778A JPS5948078B2 (en) | 1978-02-13 | 1978-02-13 | Heavy oil pyrolysis method |
| JP14127/78 | 1978-02-13 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1112198A true CA1112198A (en) | 1981-11-10 |
Family
ID=11852451
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA318,899A Expired CA1112198A (en) | 1978-02-13 | 1978-12-29 | Process for cracking heavy liquid hydrocarbons |
Country Status (5)
| Country | Link |
|---|---|
| JP (1) | JPS5948078B2 (en) |
| CA (1) | CA1112198A (en) |
| DE (1) | DE2851420A1 (en) |
| FR (1) | FR2416932A1 (en) |
| GB (1) | GB2016511B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS55102684A (en) | 1979-01-06 | 1980-08-06 | Mitsui Eng & Shipbuild Co Ltd | Thermal cracking of hydrocarbon and its device |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB447389A (en) * | 1934-08-10 | 1935-02-12 | Petrosani Societate Anonima Pe | Continual process for the transformation of liquid and solid hydrocarburets of any origin and kind into incondensable gaseous hydrocarburets without carbon deposits |
| NL267291A (en) * | 1959-05-14 | 1900-01-01 | ||
| US3252774A (en) * | 1962-06-11 | 1966-05-24 | Pullman Inc | Production of hydrogen-containing gases |
| JPS5323302A (en) * | 1976-08-18 | 1978-03-03 | Mitsui Petrochem Ind Ltd | Thermal cracking of hydrocarbons |
-
1978
- 1978-02-13 JP JP1412778A patent/JPS5948078B2/en not_active Expired
- 1978-11-14 GB GB7844468A patent/GB2016511B/en not_active Expired
- 1978-11-28 DE DE19782851420 patent/DE2851420A1/en not_active Withdrawn
- 1978-12-04 FR FR7834127A patent/FR2416932A1/en active Granted
- 1978-12-29 CA CA318,899A patent/CA1112198A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5948078B2 (en) | 1984-11-24 |
| GB2016511B (en) | 1982-04-07 |
| FR2416932B1 (en) | 1982-11-12 |
| JPS54107906A (en) | 1979-08-24 |
| FR2416932A1 (en) | 1979-09-07 |
| DE2851420A1 (en) | 1979-08-16 |
| GB2016511A (en) | 1979-09-26 |
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