[go: up one dir, main page]

US3242223A - Production of acetylene by thermal cracking of liquid hydrocarbons - Google Patents

Production of acetylene by thermal cracking of liquid hydrocarbons Download PDF

Info

Publication number
US3242223A
US3242223A US157718A US15771861A US3242223A US 3242223 A US3242223 A US 3242223A US 157718 A US157718 A US 157718A US 15771861 A US15771861 A US 15771861A US 3242223 A US3242223 A US 3242223A
Authority
US
United States
Prior art keywords
cracked
liquid
oxygen
reaction
products
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 - Lifetime
Application number
US157718A
Inventor
Nonnenmacher Helmut
Jenkner Otto
Sinn Richard
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Application granted granted Critical
Publication of US3242223A publication Critical patent/US3242223A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/22—Aliphatic unsaturated hydrocarbons containing carbon-to-carbon triple bonds
    • C07C11/24—Acetylene
    • 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
    • C10G9/36—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 with heated gases or vapours
    • C10G9/38—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 with heated gases or vapours produced by partial combustion of the material to be cracked or by combustion of another hydrocarbon

Definitions

  • This invention relates to improvements in a process for the production of acetylene by thermal cracking of liquid hydrocarbons with amounts of oxygen insuflicient for complete combustion of the hydrocarbons, and quenching of the reaction products.
  • the known processes for the cracking of hydrocarbons, to acetylene in particular therefore differ from each other not only in the particular hydrocarbon used but also especially in the method of supplying energy to the initial material and withdrawing the energy during quenching of the gas produced.
  • the energy necessary may be supplied, for example, by an electric are or by introducing vaporizable raw materials into the hot combustion products of the same or another vaporizable or gaseous fuel.
  • Processes are also known with a regenerative supply of heat to the liquid hydrocarbons.
  • Other cracking processes produce the heat required for cracking by partial combustion of part of the liquid hydrocarbons with air or oxygen within the liquid hydrocarbons to be cracked. The hydrocarbons present in excess are cracked by the combustion heat developed.
  • the subsequent rapid quenching of the hot reaction products necessary after each cracking may be effected, for example, by injecting water into the eflluent production gas. In this way, however, a very large quantity of the total energy input is lost.
  • the hydrocarbons to be cracked as the quenching agent instead of water, the said hydrocarbons being atomized into the production gas, or conversely the production gas being led directly through the liquid hydrocarbons to be cracked.
  • liquid hydrocarbons to be cracked are atomized with oxygen within a submerged bell serving as a flame chamber and ignited therein.
  • the heat reflection of the bricklined bell wall determines the stability of the flame.
  • the hydrocarbons supplied in excess to the burner nozzle are cracked.
  • the reaction gas formed passes at the lower edge of the bell into the liquid hydrocarbon phase and is thereby rapidly cooled.
  • the liquid products arising from the cracking and also the carbon black mix with the liquid ing chamber.
  • Another process for cracking liquid hydrocarbons operates without a submerged bell.
  • a submerged flame is maintained directly in the liquid hydrocarbon to be cracked.
  • the oxygen alone is led in beneath the surface of the liquid and allowed to react as a flame.
  • the reaction heat liberated in the boundary surface between the flame and the surrounding oil phase cracks the hydrocarbons.
  • the oil bottoms, to which the hydrocarbons to be cracked are added to replace the oil consumed, serves to quench the reaction products.
  • part of the suspension of finely divided carbon in the liquid hydrocarbons may be withdrawn periodically or continuously. After separation of the carbon black, the liquid hydrocarbon is returned to the reaction vessel.
  • the procedure may also be that part of the hydrocarbon containing carbon black is withdrawn from the reaction chamber and part thereof returned to the reaction chamber through the burner so that upon entry into and in the flame chamber it surrounds the oxygen.
  • the remaining considerably smaller amount of hydrocarbon containing carbon black which is 3 to 50 times the amount which could be completely burnt by the whole of the oxygen supplied to the flame chamber, is atomized in the oxygen for partial combustion.
  • a further disadvantage for example of submerged flame cracking, lies in the high expenditure for protective measures.
  • the large reaction chamber filled with the liquid hydrocarbon in which the submerged flame burns must be placed in an appropriately large concrete chamber because lasting Spontaneous ignition of the flame in a liquid system cannot be ensured.
  • the throughput itself is limited by the violence of the gas evolution which carries up the liquid from the reaction vessel.
  • the process according to this invention comprises introducing the hydrocarbons, especially petroleums, to be cracked and their liquid cracked products separately into the process, by reacting some of the liquid products containing carbon black which are formed by the cracking and are returned with oxygen in a common free space by means of a burner and supplying to the stream of the hot reaction products thus formed laterally first one or more jets of the hydrocarbon to be cracked and then, to quench the reaction mixture, one or more jets of circulated liquid cracked products containing carbon black, the laterally introduced jets having such an impact pressure that they penetrate into the stream of the reaction products and are substantially mixed therein, the amount of the hydrocarbon to be cracked being so measured that 3.0 to 1.0 'kg., preferably 2.5 to 1.5 kg.
  • liquid cracked products boiling above 85 C. formed by the cracking may be completely reacted with oxygen, they are advantageously returned to the burner in an amount of 30 to 150% of the hydrocarbons to be cracked.
  • the stream of hot reaction product formed has, prior to mixing with the hydrocarbons to be cracked, a temperature of 1200 to 2800 C., especially 1800 to 2200 C. After mixing with the hydrocarbons to be cracked, a temperature of 800 to 1600 (1., especially l000 to 1400 C, prevails. This temperature is lowered to about to 500 C. by quenching with the liquid cracked products circulated.
  • the process according to this invention can be carried out at normal or increased pressure, for example 5 to 20 atmospheres.
  • the process is not limited to pure oxygen. Diluents such as nitrogen, carbon dioxide and especially steam, may also be added to the oxygen.
  • This cracking process was first carried out on a laboratory scale with model substances in order to investigate the stable relationships of flame formation under the conditions of the reaction according to this invention.
  • model substance of the hydrocarbon to be cracked use was made of light gasoline and as model substance for the liquid cracked product, benzene.
  • the hydrocarbon to be cracked was supplied as gasoline vapour, for example, from two nozzles arranged directly opposite each other into a cold jet of oxygen, which issued from a burner into a free space at a speed of between 50 and meters per second in deficiency to the methane surrounding it after ignition.
  • the ratio of cubic meters (S.T.P.) of oxygen to kilograms of injected gasoline was between 0.5 and 0.8, the outlet speed of the gasoline jets was between 5 and 25 meters per second.
  • the production gas at 1000 to 1300 C. was quenched to about 300 C. by benzene vapour slightly above the visible reaction zone.
  • the quenched production gas was free from oxygen even when the oxygen exceeded 2.5 times the amount necessary for complete combustion of the methane.
  • the production gas obtained by quenching with benzene shows for example for a value of 0.8 cubic meter (S.T.P.) of oxygen per kilogram of injected gasoline, a percentage mole ratio of acetylene/acetylenes plus ethylene of 69.5 and a volumetric ratio of acetylenes to ethylene of 2.29 or a volumetric ratio of acetylene/ethylene plus higher C H olefines of 1.65.
  • Quenching with gasoline instead of benzene gives by comparison the values 54.0, 1.18 and 0.9.
  • a similar displacement toward a gas composition richer in olefines occurs when quenching with benzene-gasoline mixtures.
  • a burner 1 the opening of which projects upwardly into a free reaction space 2 is fed at 3 with liquid products containing carbon black originating from the cracking.
  • the necessary oxygen is supplied at 4.
  • one or more jets of the liquid hydrocarbon to be cracked are injected into the stream of hot reaction products laterally through a ring of nozzles 6.
  • the stream of the reaction products is substantially dis rupted by one or more jets of circulated liquid cracked products containing carbon black which are emitted from a ring of nozzles 7.
  • the inner walls of reaction chamber 2 are rinsed with liquid cracked products from the top through a hollow cone nozzle 8.
  • the cooled production gas leaves the reaction chamber at 9 together with the liquid products and flows through a pipe 10 to a washing and cooling zone 11 into the top of which phlegm gasoline is pumped through a pipe 12 for evaporation cooling.
  • a pipe 10 which is provided with a dip leg into bottom 14 of column 11 and the gaseous and vaporous products leave the reaction chamber above the quenching jets 7 through a pipe (not shown) which opens into bottom 14 above the level of the liquid therein. Additional heat may be withdrawn from the column 11 by a waste heat boiler 13 attached to bottom 14.
  • the column is so operated that the level of the bottoms circulated through the pipes 15, 16, 17, 18, 9 and 10 and container 14 remains constant.
  • the cooled production gas freed for the most part from carbon black, leaves the apparatus at for further working up in an attached apparatus 19.
  • Example 17 kg. per hour of liquid cracked product containing carbon black is supplied to burner 1 from container 14 and at the same time, for intimate mixing, 15 cubic meters (S.T.P.) of oxygen per hour is supplied to the burner. As the mixture enters the reaction chamber 2 it is ignited by pilot flames 5 fed with fuel gas and oxygen. 25 kg. of crude oil per hour is injected through jets 6 into the stream of hot reaction products formed, for the purpose of cracking. After a cracking period of about 0.003 second, the reaction products are quenched by circulated liquid cracked products containing carbon black to 250 C., by supplying about 1000 kg. of hottoms per hour from container 14 through pipes 15 and 17 to the quenching jets 7.
  • S.T.P. 15 cubic meters
  • the vessel walls are rinsed with 100 kg. of bottoms (per hour) atomized by means of the hollow cone nozzle 8.
  • the quenched gas and vapour pass together with liquid products through pipe 10 into column 11. 1 kg. of bottoms is withdrawn per hour from 14 through the pipe 21.
  • a process for the production of acetylene by thermal cracking of liquid hydrocarbons with amounts of oxygen insuflicient for complete combustion and quenching of the reaction products wherein part of the liquid product containing carbon black formed by the cracking and recycled is brought to reaction with oxygen in a common free space by means of a burner and into the stream of the hot reaction products thereby formed there is supplied laterally first at least one jet of the hydrocarbon to be cracked and then, for the quenching of the reaction mixture, at least one jet of circulated liquid cracked products containing carbon black, the laterally-introduced jets having such an impact pressure that they penetrate the stream of reaction products and are substantially mixed therein, the amount of the hydrocarbon to be cracked being such that 3.0 to 1.0 kg.
  • a process as claimed in claim 1 wherein the amount of the hydrocarbon mixture to be cracked is such that 2.5 to 1.5 kg. of the hydrocarbon mixture to be cracked is used for every cubic meter (S.T.P.) of oxygen.
  • a process as claimed in claim 1 wherein the stream of hot reaction products has a temperature of from 1200 to 2800 C. prior to mixing with said hydrocarbon to be cracked; has a temperature of from 800 to 1600 C. after mixing with said hydrocarbon to be cracked; and has a temperature of from to 500 C. after mixing with said quench liquid consisting of circulated. liquid cracked products containing carbon black.
  • a process as in claim 4 wherein the stream of hot reaction products has a temperature of from 1800 to 2200 C. prior to mixing with said hydrocarbon to be cracked; has a temperature of from 1000 to 1400 C. after mixing with said hydrocarbon to be cracked; and has a temperature of from 100 to 500 C. after mixing with said quench liquid consisting of circulated liquid cracked products containing carbon black.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Description

a h 22. 1966 H. NONNENMACHER ETAL 3,242,223
PRODUCTION OF ACETYLENE BY THERMAL CRACKING OF LIQUID HYDROGARBONS Filed D80. 7, 1961 INVENTORS; HELMUT NONNENMACHER OTTO JENKNER RICHARD SINN I I m5? United States Patent PRODUCTION OF ACETYLENE BY THERMAL CRACKING 0F LIQUID HYDROCARBONS Helmut Nonnenmacher, Ludwigshafen (Rhine), Otto Jenlmer, Mannheim, and Richard Sinn, Ludwigshafen (Rhine), Germany, assignors to Badische Anilin- & Soda-Fabrik Aktiengesellschaft, Ludwigshafen (Rhine), Germany Filed Dec. 7, 1961, Ser. No. 157,718
Claims priority, application Germany, Dec. 10, 1960,
5 Claims. (Cl. 260-679) This invention relates to improvements in a process for the production of acetylene by thermal cracking of liquid hydrocarbons with amounts of oxygen insuflicient for complete combustion of the hydrocarbons, and quenching of the reaction products.
More especially, it relates to the introduction of liquid hydrocarbons and their liquid cracked products into the process and to the circulation of liquid cracked products for quenching the reaction mixture.
It is known to crack hydrocarbons into unsaturated gaseous products, especially acetylene, by the supply of energy. On the other hand substantial energy must immediately be withdrawn from the cracked products formed at high temperature in order to prevent further decomposition and side reactions.
The known processes for the cracking of hydrocarbons, to acetylene in particular, therefore differ from each other not only in the particular hydrocarbon used but also especially in the method of supplying energy to the initial material and withdrawing the energy during quenching of the gas produced.
To crack liquid hydrocarbons, the energy necessary may be supplied, for example, by an electric are or by introducing vaporizable raw materials into the hot combustion products of the same or another vaporizable or gaseous fuel. Processes are also known with a regenerative supply of heat to the liquid hydrocarbons. Other cracking processes produce the heat required for cracking by partial combustion of part of the liquid hydrocarbons with air or oxygen within the liquid hydrocarbons to be cracked. The hydrocarbons present in excess are cracked by the combustion heat developed.
The subsequent rapid quenching of the hot reaction products necessary after each cracking may be effected, for example, by injecting water into the eflluent production gas. In this way, however, a very large quantity of the total energy input is lost. In order to make the sensible heat of the production gas utilisable for preheating the input substance, it has also been proposed to use the hydrocarbons to be cracked as the quenching agent instead of water, the said hydrocarbons being atomized into the production gas, or conversely the production gas being led directly through the liquid hydrocarbons to be cracked.
From this further diiferences arise in carrying out the thermal cracking of liquid hydrocarbons by partial combustion.
It is known to maintain a flame below the surface of liquid hydrocarbons, especially mineral oils. For this purpose the liquid hydrocarbons to be cracked are atomized with oxygen within a submerged bell serving as a flame chamber and ignited therein. The heat reflection of the bricklined bell wall determines the stability of the flame. In the course of the partial combustion, the hydrocarbons supplied in excess to the burner nozzle are cracked. The reaction gas formed passes at the lower edge of the bell into the liquid hydrocarbon phase and is thereby rapidly cooled. The liquid products arising from the cracking and also the carbon black mix with the liquid ing chamber.
Another process for cracking liquid hydrocarbons operates without a submerged bell. A submerged flame is maintained directly in the liquid hydrocarbon to be cracked. In one embodiment, the oxygen alone is led in beneath the surface of the liquid and allowed to react as a flame. The reaction heat liberated in the boundary surface between the flame and the surrounding oil phase cracks the hydrocarbons. The oil bottoms, to which the hydrocarbons to be cracked are added to replace the oil consumed, serves to quench the reaction products. In order to control the carbon black content of the oil bottoms, for example, part of the suspension of finely divided carbon in the liquid hydrocarbons may be withdrawn periodically or continuously. After separation of the carbon black, the liquid hydrocarbon is returned to the reaction vessel. The procedure may also be that part of the hydrocarbon containing carbon black is withdrawn from the reaction chamber and part thereof returned to the reaction chamber through the burner so that upon entry into and in the flame chamber it surrounds the oxygen. The remaining considerably smaller amount of hydrocarbon containing carbon black, which is 3 to 50 times the amount which could be completely burnt by the whole of the oxygen supplied to the flame chamber, is atomized in the oxygen for partial combustion.
For the thermal cracking of liquid hydrocarbons it has also been proposed to atomize them in a free reaction chamber with amounts of oxygen insuflicient for combustion and to allow them to react after ignition. This process makes use of a special direct method of quenching the reaction mixture which consists of the combustion gases and cracked gases, with the hydrocarbons that are used for cracking. This consists in atomizing such an excess of liquid hydrocarbons with the oxygen prior to combustion and cracking that simultaneous quenching of the reaction gas is made possible. In stationary operation, the atomizing nozzle is fed with the products of the bottoms collecting in the reaction vessel with an admixture of initial oil to replace the amount of hydrocarbon used up.
One characteristic common to all the said processes for the thermal cracking of liquid hydrocarbons by partial combustion is, that in carrying them out, the actual liquid raw material to be cracked and the liquid products of the reaction are introduced into the process not separately but mixed with one another. The acetylene of the production gases therefore collects for working up in a diluted condition by reason of a considerable content of olefinic gases, especially ethylene. The undesirably large portion of olefinic gases is the result of subsequent cracking reactions which may occur during the quenching process at lower temperatures than of the original cracking, with hydrocarbons of the quenching 'liquid.
The higher utilization of energy by the conversion of sensible heat into chemical energy of additional olefinic cracked products is counteracted, however, by the separation of acetylene from the production gas which is more strongly troubled by the increased content of olefines. Moreover, a lean gas is obtained in the acetylene separation which is still considerably enriched in olefines and must be separated from the olefines in a further step.
A process for the cracking of liquid hydrocarbons which yielded a production gas rich in acetylene but poor in olefines would therefore offer advantages over the known DrOCesses.
A further disadvantage, for example of submerged flame cracking, lies in the high expenditure for protective measures. Thus the large reaction chamber filled with the liquid hydrocarbon in which the submerged flame burns must be placed in an appropriately large concrete chamber because lasting Spontaneous ignition of the flame in a liquid system cannot be ensured. The throughput itself is limited by the violence of the gas evolution which carries up the liquid from the reaction vessel. These disadvantages interfere with every enlargement of the scale on which the process is to be carried out.
Since, because of their ash content, the combustion of cracked oils in combustion chambers leads, in the long run, to total destruction of the walls the known processes which supply the necessary cracking energy in the form of hot fuel gas, make use of the combustion of gaseous or readily, vaporizable hydrocarbons. On account of the technical difliculties which interfere with a return of residues from petroleum cracking for combustion in combustion chambers, only gaseous or vaporized hydrocarbons of light to medium petroleum fractions are used for cracking in the reactor which is arranged after the combustion chamber. The exclusion of crude oils from cracking is a disadvantage of this process.
We have now found for the production of acetylene by thermal cracking of liquid hydrocarbons, especially hydrocarbon mixtures containing unvaporizable constituents, for example crude oils, which avoids the said disadvantages and, in contrast to the known processes, yields a production gas which by reason of its lower olefine content permits a more ready separation of the acetylene from the production gas. Moreover, the residual gas poor in olefines, since it, is not subjected to any further separation, can also be converted in a simple way, for example by flameless cracking with oxygen, into synthesis gas.
The process according to this invention comprises introducing the hydrocarbons, especially petroleums, to be cracked and their liquid cracked products separately into the process, by reacting some of the liquid products containing carbon black which are formed by the cracking and are returned with oxygen in a common free space by means of a burner and supplying to the stream of the hot reaction products thus formed laterally first one or more jets of the hydrocarbon to be cracked and then, to quench the reaction mixture, one or more jets of circulated liquid cracked products containing carbon black, the laterally introduced jets having such an impact pressure that they penetrate into the stream of the reaction products and are substantially mixed therein, the amount of the hydrocarbon to be cracked being so measured that 3.0 to 1.0 'kg., preferably 2.5 to 1.5 kg. of the hydrocarbon to be cracked is used for every cubic meter (S.T.P.) of oxygen, and the amount of cracked product circulated and used for quenching the reaction mixture being sufficient to decrease the temperature of the reaction mixture to below 500 C. It has been found that for a rapid mixing of the jets by intersection of the jets the product of the ratio of the impact pressure of the lateral jets to the impact pressure of the reaction products, both measured at the point of penetration, and the corresponding ratio of the jet diameters must lie within the range of 0.01 to 3, especially at 0.02 to 1.
In order that the liquid cracked products boiling above 85 C. formed by the cracking may be completely reacted with oxygen, they are advantageously returned to the burner in an amount of 30 to 150% of the hydrocarbons to be cracked.
The stream of hot reaction product formed has, prior to mixing with the hydrocarbons to be cracked, a temperature of 1200 to 2800 C., especially 1800 to 2200 C. After mixing with the hydrocarbons to be cracked, a temperature of 800 to 1600 (1., especially l000 to 1400 C, prevails. This temperature is lowered to about to 500 C. by quenching with the liquid cracked products circulated.
The process according to this invention can be carried out at normal or increased pressure, for example 5 to 20 atmospheres.
The process is not limited to pure oxygen. Diluents such as nitrogen, carbon dioxide and especially steam, may also be added to the oxygen.
It is also possible to supply carbon dioxide or steam to the reaction chamber together with or separately from the hydrocarbons to be cracked and/or with the cracked products used for quenching, mixing with the reaction products or reaction mixture being effected by intersection of streams.
This cracking process was first carried out on a laboratory scale with model substances in order to investigate the stable relationships of flame formation under the conditions of the reaction according to this invention. As model substance of the hydrocarbon to be cracked use was made of light gasoline and as model substance for the liquid cracked product, benzene.
The hydrocarbon to be cracked Was supplied as gasoline vapour, for example, from two nozzles arranged directly opposite each other into a cold jet of oxygen, which issued from a burner into a free space at a speed of between 50 and meters per second in deficiency to the methane surrounding it after ignition. The ratio of cubic meters (S.T.P.) of oxygen to kilograms of injected gasoline was between 0.5 and 0.8, the outlet speed of the gasoline jets was between 5 and 25 meters per second. The production gas at 1000 to 1300 C. was quenched to about 300 C. by benzene vapour slightly above the visible reaction zone.
The quenched production gas was free from oxygen even when the oxygen exceeded 2.5 times the amount necessary for complete combustion of the methane.
The safety in operation of the process as compared with those in which accumulations of oxygen can occur in the production gas becomes obvious in the extreme case when the oxygen flows into the reaction chamber without methane. Even under such conditions, the cold oxygen may be completely reacted with the injected hydrocarbons in a short flame. During this experiment, to maintain the flame, a small pilot flame burned in the direction of the mixing point of the oxygen and gasoline vapour. The product of the ratio of the impact pressure of the gasoline vapour jet to that of the oxygen jet and the corresponding ratio of the jet diameters lies between 0.004 and 0.4 at the point of mixing. The production gas also remained free from oxygen when the supply of benzene or of gasoline vapour to the reaction vessel was interrupted at will.
The production gas obtained by quenching with benzene shows for example for a value of 0.8 cubic meter (S.T.P.) of oxygen per kilogram of injected gasoline, a percentage mole ratio of acetylene/acetylenes plus ethylene of 69.5 and a volumetric ratio of acetylenes to ethylene of 2.29 or a volumetric ratio of acetylene/ethylene plus higher C H olefines of 1.65. Quenching with gasoline instead of benzene gives by comparison the values 54.0, 1.18 and 0.9. A similar displacement toward a gas composition richer in olefines occurs when quenching with benzene-gasoline mixtures.
An apparatus suitable for carrying out the process according to this invention is illustrated by way of example in the accompanying diagrammatic drawing. A burner 1, the opening of which projects upwardly into a free reaction space 2 is fed at 3 with liquid products containing carbon black originating from the cracking. The necessary oxygen is supplied at 4. After the mixture has been ignited by one or more pilot flames 5, one or more jets of the liquid hydrocarbon to be cracked are injected into the stream of hot reaction products laterally through a ring of nozzles 6. To quench the hot reaction products, the stream of the reaction products, after a short reaction period, is substantially dis rupted by one or more jets of circulated liquid cracked products containing carbon black which are emitted from a ring of nozzles 7. The inner walls of reaction chamber 2 are rinsed with liquid cracked products from the top through a hollow cone nozzle 8.
The cooled production gas leaves the reaction chamber at 9 together with the liquid products and flows through a pipe 10 to a washing and cooling zone 11 into the top of which phlegm gasoline is pumped through a pipe 12 for evaporation cooling. In many cases it is advantageous to supply the cooled production gas and vapour to the column separately from the liquid products. The liquid products then flow through pipe 10 which is provided with a dip leg into bottom 14 of column 11 and the gaseous and vaporous products leave the reaction chamber above the quenching jets 7 through a pipe (not shown) which opens into bottom 14 above the level of the liquid therein. Additional heat may be withdrawn from the column 11 by a waste heat boiler 13 attached to bottom 14. The column is so operated that the level of the bottoms circulated through the pipes 15, 16, 17, 18, 9 and 10 and container 14 remains constant.
The cooled production gas, freed for the most part from carbon black, leaves the apparatus at for further working up in an attached apparatus 19.
Bottoms oil is withdrawn through a pipe 21 for the removal of ash.
This invention is illustrated by, but not limited to, the following example, given with reference to the drawing.
Example 17 kg. per hour of liquid cracked product containing carbon black is supplied to burner 1 from container 14 and at the same time, for intimate mixing, 15 cubic meters (S.T.P.) of oxygen per hour is supplied to the burner. As the mixture enters the reaction chamber 2 it is ignited by pilot flames 5 fed with fuel gas and oxygen. 25 kg. of crude oil per hour is injected through jets 6 into the stream of hot reaction products formed, for the purpose of cracking. After a cracking period of about 0.003 second, the reaction products are quenched by circulated liquid cracked products containing carbon black to 250 C., by supplying about 1000 kg. of hottoms per hour from container 14 through pipes 15 and 17 to the quenching jets 7. To avoid deposits of carbon black in the reaction chamber, the vessel walls are rinsed with 100 kg. of bottoms (per hour) atomized by means of the hollow cone nozzle 8. The quenched gas and vapour pass together with liquid products through pipe 10 into column 11. 1 kg. of bottoms is withdrawn per hour from 14 through the pipe 21.
By cracking 25 kg. of crude oil, 43 cubic meters (S.T.P.) of cracked gas is obtained which contains 11.0% by volume of acetylene and 4.5% by volume of olefinic hydrocarbons. The remaining gas consists mainly of carbon monoxide and hydrogen.
What we claim is:
1. A process for the production of acetylene by thermal cracking of liquid hydrocarbons with amounts of oxygen insuflicient for complete combustion and quenching of the reaction products, wherein part of the liquid product containing carbon black formed by the cracking and recycled is brought to reaction with oxygen in a common free space by means of a burner and into the stream of the hot reaction products thereby formed there is supplied laterally first at least one jet of the hydrocarbon to be cracked and then, for the quenching of the reaction mixture, at least one jet of circulated liquid cracked products containing carbon black, the laterally-introduced jets having such an impact pressure that they penetrate the stream of reaction products and are substantially mixed therein, the amount of the hydrocarbon to be cracked being such that 3.0 to 1.0 kg. of the hydrocarbon mixture which is to be cracked and which contains unvaporizable constituents is used for every cubic meter (S.T.P.) of oxygen, and the amount of cracked product circulated and used for quenching the reaction mixture being suflicient to lower the temperature of the reaction mixture to below 500 C.
2. A process as claimed in claim 1 wherein the amount of the hydrocarbon mixture to be cracked is such that 2.5 to 1.5 kg. of the hydrocarbon mixture to be cracked is used for every cubic meter (S.T.P.) of oxygen.
3. A process as claimed in claim 1 wherein the products boiling above C. formed in the cracking are returned to the burner in an amount of 30 to 150% of the hydrocarbon mixture to be cracked.
4. A process as claimed in claim 1 wherein the stream of hot reaction products has a temperature of from 1200 to 2800 C. prior to mixing with said hydrocarbon to be cracked; has a temperature of from 800 to 1600 C. after mixing with said hydrocarbon to be cracked; and has a temperature of from to 500 C. after mixing with said quench liquid consisting of circulated. liquid cracked products containing carbon black.
5. A process as in claim 4 wherein the stream of hot reaction products has a temperature of from 1800 to 2200 C. prior to mixing with said hydrocarbon to be cracked; has a temperature of from 1000 to 1400 C. after mixing with said hydrocarbon to be cracked; and has a temperature of from 100 to 500 C. after mixing with said quench liquid consisting of circulated liquid cracked products containing carbon black.
References Cited by the Examiner UNITED STATES PATENTS 2,520,149 8/1950 Keeling 260-679 2,985,695 5/1961 Platz et al. 260-679 2,985,698 5/1961 Pechtold et al. 260-679 3,022,148 2/1962 James 260-679 XR 3,051,639 8/1962 Anderson 260-679 3,140,323 7/1964 Fauser 260-679 FOREIGN PATENTS 461,497 2/ 1937 Great Britain.
ALPHONSO D. SULLIVAN, Primary Examiner.

Claims (1)

1. A PROCESS FOR THE PRODUCTION OF ACETYLENE BY THERMAL CRACKING OF LIQUID HYDROCARBONS WITH AMOUNTS OF OXYGEN INSUFFICIENT FOR COMPLETE COMBUSTION AND QUENCHING OF THE REACTION PRODUCTS, WHEREIN PART OF THE LIQUID PRODUCT CONTAINING CARBON BLACK FORMED BY THE CRACKING AND RECYCLED IS BROUGHT TO REACTION WITH OXYGEN IN A COMMON FREE SPACE BY MEANS OF A BURNER AND INTO THE STREAM OF THE HOT REACTION PRODUCTS THEREBY FORMED THERE IS SUPPLIED LATERALLY FIRST AT LEAST ONE JET OF THE HYDROCARBON TO BE CRACKED AND THEN, FOR THE QUENCHING OF THE REACTION MIXTURE, AT LEAST ONE JET OF CIRCULATED LIQUID CRACKED PRODUCTS CONTAINING CARBON BLACK, THE LATERALLY-INTRODUCED JETS HAVING SUCH AN IMPACT PRESSURE THAT THEY PENETRATE THE STREAM OF REACTION PRODUCTS AND ARE SUBSTANTIALLY MIXED THEREIN, THE AMOUNT OF THE HYDROCARBON TO BE CRACKED BEING SUCH THAT 3.0 TO 1.0 KG. OF THE HYDROCARBON MIXTURE WHICH IS TO BE CRACKED AND WHICH CONTAINS UNVAPORIZABLE CONSTITUENTS IS USED FOR EVRY CUBIC METER (S.T.P.) OF OXYGEN, AND THE AMOUNT OF CRACKED PRODUCT CIRCULATED AND USED FOR QUENCHING THE REACTION MIXTURE BEING SUFFICIENT TO LOWER THE TEMPERATURE OF THE REACTION MIXTURE TO BELOW 500*C.
US157718A 1960-12-10 1961-12-07 Production of acetylene by thermal cracking of liquid hydrocarbons Expired - Lifetime US3242223A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DEB60428A DE1144260B (en) 1960-12-10 1960-12-10 Process for the production of acetylene by thermal cracking of liquid hydrocarbons

Publications (1)

Publication Number Publication Date
US3242223A true US3242223A (en) 1966-03-22

Family

ID=6972821

Family Applications (1)

Application Number Title Priority Date Filing Date
US157718A Expired - Lifetime US3242223A (en) 1960-12-10 1961-12-07 Production of acetylene by thermal cracking of liquid hydrocarbons

Country Status (4)

Country Link
US (1) US3242223A (en)
DE (1) DE1144260B (en)
FR (1) FR1307779A (en)
GB (1) GB926896A (en)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012099677A2 (en) 2011-01-19 2012-07-26 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
US20130204055A1 (en) * 2011-08-25 2013-08-08 S. Mark Davis Selective Hydrogenation of Alkynyl-Containing Compounds and Polyunsaturated Compounds
US9187699B2 (en) 2011-11-08 2015-11-17 Exxonmobil Chemical Patents Inc. Hydrocarbon pyrolysis process
US9346728B2 (en) 2011-01-19 2016-05-24 Exxonmobil Chemical Patents Inc. Hydrocarbon conversion process
US9505680B2 (en) 2011-01-19 2016-11-29 Exxonmobil Chemical Patents Inc. Method and apparatus for managing the conversion of hydrocarbons into olefins
US9663419B2 (en) 2011-01-19 2017-05-30 Exxonmobil Chemical Patents Inc. Hydrocarbon conversion process
US9677014B2 (en) 2011-01-19 2017-06-13 Exxonmobil Chemical Patents Inc. Process and apparatus for converting hydrocarbons
US9676681B2 (en) 2011-01-19 2017-06-13 Exxonmobil Chemical Patents Inc. Method and apparatus for managing hydrogen content through the conversion of hydrocarbons into olefins
US9708232B2 (en) 2011-01-19 2017-07-18 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
US9708231B2 (en) 2011-01-19 2017-07-18 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins using hydroprocessing and thermal pyrolysis
US9809508B2 (en) 2011-01-19 2017-11-07 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
US9815751B2 (en) 2011-01-19 2017-11-14 Exxonmobil Chemical Patents Inc. Hydrocarbon and oxygenate conversion by high severity pyrolysis to make acetylene and ethylene
US9868680B2 (en) 2011-01-19 2018-01-16 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3393250A (en) * 1965-04-15 1968-07-16 Lummus Co Process for producing unsaturated compounds

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB461497A (en) * 1935-07-17 1937-02-17 Ig Farbenindustrie Ag Improvements in and apparatus for the manufacture and production of carbon black
US2520149A (en) * 1944-06-14 1950-08-29 Koppers Co Inc Process for producing olefins
US2985698A (en) * 1957-09-27 1961-05-23 Hoechst Ag Process for pyrolyzing hydrocarbons
US2985695A (en) * 1957-01-11 1961-05-23 Basf Ag Cracking of hydrocarbons
US3022148A (en) * 1958-11-18 1962-02-20 Chemical Construction Corp Oil quench process for partial oxidation of hydrocarbon gases
US3051639A (en) * 1958-09-25 1962-08-28 Union Carbide Corp Arc torch chemical reactions
US3140323A (en) * 1958-05-21 1964-07-07 Montedison Spa Process for production of acetylene and other products by partial combustion of hydrocarbons

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1014275B (en) * 1955-07-14 1957-08-22 Huels Chemische Werke Ag Process for the thermal cracking of liquid hydrocarbons
GB795688A (en) * 1955-09-30 1958-05-28 Huels Chemische Werke Ag Improvements in the thermal cracking of combustible organic liquids
GB802226A (en) * 1956-08-14 1958-10-01 Huels Chemische Werke Ag Improvements in the thermal cracking of liquid hydrocarbons
DE1059898B (en) * 1958-01-07 1959-06-25 Basf Ag Process for splitting hydrocarbons

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB461497A (en) * 1935-07-17 1937-02-17 Ig Farbenindustrie Ag Improvements in and apparatus for the manufacture and production of carbon black
US2520149A (en) * 1944-06-14 1950-08-29 Koppers Co Inc Process for producing olefins
US2985695A (en) * 1957-01-11 1961-05-23 Basf Ag Cracking of hydrocarbons
US2985698A (en) * 1957-09-27 1961-05-23 Hoechst Ag Process for pyrolyzing hydrocarbons
US3140323A (en) * 1958-05-21 1964-07-07 Montedison Spa Process for production of acetylene and other products by partial combustion of hydrocarbons
US3051639A (en) * 1958-09-25 1962-08-28 Union Carbide Corp Arc torch chemical reactions
US3022148A (en) * 1958-11-18 1962-02-20 Chemical Construction Corp Oil quench process for partial oxidation of hydrocarbon gases

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9676681B2 (en) 2011-01-19 2017-06-13 Exxonmobil Chemical Patents Inc. Method and apparatus for managing hydrogen content through the conversion of hydrocarbons into olefins
US9708232B2 (en) 2011-01-19 2017-07-18 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
US9868680B2 (en) 2011-01-19 2018-01-16 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
US9815919B2 (en) 2011-01-19 2017-11-14 Exxonmobil Chemical Patents Inc. Hydrocarbon conversion process
US9346728B2 (en) 2011-01-19 2016-05-24 Exxonmobil Chemical Patents Inc. Hydrocarbon conversion process
US9505680B2 (en) 2011-01-19 2016-11-29 Exxonmobil Chemical Patents Inc. Method and apparatus for managing the conversion of hydrocarbons into olefins
US9815751B2 (en) 2011-01-19 2017-11-14 Exxonmobil Chemical Patents Inc. Hydrocarbon and oxygenate conversion by high severity pyrolysis to make acetylene and ethylene
US9663419B2 (en) 2011-01-19 2017-05-30 Exxonmobil Chemical Patents Inc. Hydrocarbon conversion process
WO2012099677A2 (en) 2011-01-19 2012-07-26 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
US9677014B2 (en) 2011-01-19 2017-06-13 Exxonmobil Chemical Patents Inc. Process and apparatus for converting hydrocarbons
US9708231B2 (en) 2011-01-19 2017-07-18 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins using hydroprocessing and thermal pyrolysis
US9809508B2 (en) 2011-01-19 2017-11-07 Exxonmobil Chemical Patents Inc. Method and apparatus for converting hydrocarbons into olefins
US20130204055A1 (en) * 2011-08-25 2013-08-08 S. Mark Davis Selective Hydrogenation of Alkynyl-Containing Compounds and Polyunsaturated Compounds
US9233893B2 (en) * 2011-08-25 2016-01-12 Exxonmobil Chemical Patents Inc. Selective hydrogenation of alkynyl-containing compounds and polyunsaturated compounds
US9187699B2 (en) 2011-11-08 2015-11-17 Exxonmobil Chemical Patents Inc. Hydrocarbon pyrolysis process
US10570345B2 (en) 2011-11-08 2020-02-25 Exxonmobil Chemical Patents Inc. Regenerative reactor system

Also Published As

Publication number Publication date
GB926896A (en) 1963-05-22
FR1307779A (en) 1962-10-26
DE1144260B (en) 1963-02-28

Similar Documents

Publication Publication Date Title
US3242223A (en) Production of acetylene by thermal cracking of liquid hydrocarbons
US4264435A (en) Crude oil cracking using partial combustion gases
US4725349A (en) Process for the selective production of petrochemical products
US2823243A (en) Process and apparatus for pyrolysis of hydrocarbons
US4952743A (en) Process and apparatus for the conversion of hydrocarbons
IE50171B1 (en) Method of producing olefins and other petrochemicals from hydrocarbons
US2599981A (en) Carbon black
US2623811A (en) Process for producing carbon black and valuable by-product gases
US20020064741A1 (en) Premixing burner block for partial oxidation processes
US1823503A (en) Manufacture of unsaturated hydrocarbons
US3644555A (en) Process for the production of acetylene or acetylene and ethylene by pyrolysis of hydrocarbons
JPS59152992A (en) Thermal decomposition for producing olefin from hydrocarbon
US3542894A (en) Production of acetylene
US4007017A (en) Production of clean synthesis or fuel gas
EP0059772B1 (en) Crude oil cracking using partial combustion gases
US3246957A (en) Apparatus for acetylene production by partial combustion of hydrocarbons
US3244765A (en) Production of acetylene and olefins by partial combustion of hydrocarbons
US3090684A (en) Conversion of oils with amounts of oxygen insufficient for complete combustion for the formation of carbon monoxide and hydrogen
GB929136A (en) Improvements in or relating to the production of acetylene and ethylene
US3248447A (en) Production of acetylene and ethylene by incomplete combustion of hydrocarbons
GB851994A (en) Process and apparatus for the conversion of hydrocarbons
US3242224A (en) Production of acetylene
US2905544A (en) Suspension process for the production of co and h2 from a solid carbonaceous fuel, oxygen and steam
US2734811A (en) Method for the production of fuel gas from liquid fuels
SU416956A3 (en)