US3692862A

US3692862A - Method for pyrolyzing hydrocarbons

Info

Publication number: US3692862A
Application number: US61144A
Authority: US
Inventors: Miloslav Staud; Anatolij Lazarev
Original assignee: CHEPOS Z CHEMICKEHO A POTRA VI
Current assignee: CHEPOS Z CHEMICKEHO A POTRA VI; CHEPOS ZAVODY CHEMICKEHO A POTRA-VINARSKEHO STROJIRENSTVI GENERALNI
Priority date: 1966-10-14
Filing date: 1970-08-05
Publication date: 1972-09-19
Anticipated expiration: 1989-09-19
Also published as: GB1178449A; DE1643811A1; US3563709A; FR1555656A

Abstract

A hydrocarbon raw material is pyrolyzed to lower unsaturated aliphatic hydrocarbons by mixing the raw material with hot combustion gases at a rate sufficient to heat the mixture above the pyrolyzing temperature. The endothermic reaction is performed in a porous tube while oxygen is being forced into the tube through the wall to supply the thermal energy consumed and to maintain the pyrolysis temperature by oxidation of a portion of the pyrolysis product, particularly hydrogen. The reaction mixture is then quickly cooled.

Description

United States Patent Staud et al. 1 1 Sept. 19, 1972 METHOD FOR PYROLYZING [56] References Cited HYDROCARBONS UNITED STATES PATENTS [72] Invent: gi'gfg i'g g s mg g 1,808,168 6/1931 Hopkins .....260/683.3 2,174,288 9/1939 Klein et al. ..260/683.3 [73] Assignee: Chepos, Zavody Chemickeho :1 2,387,731 10/1945 Allen ..260/680 potra-vinarskeho strojirenstvi, 2,790,838 4/1957 Schrader ..260/683 generalni, Brno, Czechoslovakia 3,161,695 12/1964 Goffinet ..260/679 3,361,839 l/1968 Lester ..260/669 [22] 1970 3,375,288 3/1968 Rosset ..260/669 21 Appl. No.2 61,144 V Primary ExaminerDelbert E. Gantz Related Apphcaflon Data Assistant Examiner-C. E. Spresser [60] Division of Ser. NO. 760,240, Sept. 17, 1968, ArwmeyRiehard Low and Murray Schaffer Pat. No. 3,563,709, and a continuation-in-part Of Ser. N0. 674,570, OCI. 11, 1967, abandoned. ABSTRACT A hydrocarbon raw material is pyrolyzed to lower un- [30] Fm'e'gn Apphcauon Pnomy Dam saturated aliphatic hydrocarbons by mixing the raw Oct. 14, 1966 Czechoslo ki 6535 66 material with hot combustion gases at a rate sufficient to heat the mixture above the pyrolyzing temperature. 521 US. Cl. ..260/683 R, 48/D1G. 5, 260/679 R, The endothermic reaction is performed in a porous 260/ 0 R 26()/633 3 tube while oxygen is being forced into the tube 51 1m. (:1 ..C07c 3/30 through the to pp y the thermal gy [58] Field 61 Search ..260/683, 679, 683.3, 680; Sumed and to maintain the Py y temperature y 43 1 5 oxidation of a portion of the pyrolysis product, particularly hydrogen. The reaction mixture is then quickly cooled.

6 Claims, 2 Drawing Figures METHOD FOR PYROLYZING HYDROCARBONS tion, Ser. No. 674,570, filed on Oct. 11, 1967, now

abandoned.

This invention relates to the pyrolysis of hydrocarbons to unsaturated aliphatic hydrocarbons having fewer carbon atoms, and particularly to a pyrolyzing method for performing the same.

It is known to mix a hydrocarbon raw material with gaseous combustionproducts in order quickly to raise the raw material to a temperature at which pyrolytic decomposition takes place. The ensuing reaction is endothermic so that the temperature of the raw material quickly reaches a maximum during mixing with the combustion gases, but then drops. Yet, it is known that the most desirable pyrolysis products are obtained by maintaining the temperature or by even gradually increasing the temperature during pyrolysis. The aforedescribed known process cannot achieve optimum results and the formation of carbonaceous solids in substantial amounts cannot be avoided.

It is also known to raise the temperature of the raw material while the same passes through a tube having a porous wall. Either a hot combustion gas or oxygen is forced into the tube under pressure. If oxygen is so admixed to the hydrocarbon, combustion of the latter provides the heat for reaching pyrolysis temperature and the formation of carbonaceous deposits on the reaction vessel is prevented. If hot combustion gas or oxygen is supplied through the permeable walls of a conduit holding the flowing raw material, the latter can be heated only relatively slowly. It dwells for relatively long periods in zones where the temperature is sufficiently below the proper pyrolysis temperature to favor the formation of undesirable by-products. Moreover, it has not been practical to build such permeable, tubular conduits of a size useful in industrial production. A sizable portion of the space in the reaction chamber actually serves as a preheating chamber. If hot combustion gases are forced into the chamber through the wall, the thermal losses significantly effect the cost of operation. I

Attempts at overcoming the difficulties outlined above have been hampered by the high cost of materials capable of withstanding the temperatures necessary for pyrolysis and the even higher cost of shaping such materials.

A primaryobject of the invention is the provision of a continuous pyrolysis method for a hydrocarbon raw material in which the temperature can be controlled at will along the stream of reactants, more particularly, the raw material is heated almost instantaneously to the pyrolysis temperature, and the thermal energy consumed by the endothermic reaction is replenished as needed to provide constant or even rising temperature through the reaction zone. Another object is the provision of reliable and practical apparatus for performing the method.

In the method of the invention, a stream of fuel is burned with an oxygen-bearing gas to produce a stream of hot combustion gas. The latter is mixed with a stream of the hydrocarbon raw material to be pyrolyzed at a rate sufficient to raise the temperature of the mixture so produced to the pyrolysis temperature of the raw material. The mixture is then passed through a conduit having a porous wall while at pyrolysis temperature, whereby a major portion of the raw material is thermally decomposed in the conduit. An additional and secondary amount of oxygen bearing gas is introduced inward of the conduit through the porous wall at a rate sufficient to supply the thermal energy consumed by the endothermic pyrolysis reaction, whereby the temperature is at least substantially maintained, but may be increased by oxidation of a portion of the reaction products. The remainder of the products is then withdrawn from the conduit.

The apparatus employed includes the burner required for burning the fuel, a reaction chamber having a wall of permeable material, and a source of hydrocarbon raw material. A mixing device is interposed between the burner and the reaction chamber and is connected to the raw material source for receiving the combustion gas and the raw material, mixing the same, and discharging the mixture so produced into the reaction chamber. A pressure chamber is in contact with a face of the aforementioned wall outside the reaction chamber and means are provided for feeding an oxygen bearing gas to the pressure chamber. The reaction chamber has an outlet for discharge of a reaction mixture formed therein, and a cooling device is provided for cooling the discharged reaction mixture.

Further objects, additional features, and many of the attendant advantages of this invention will readily be appreciated as the same becomes better understood by the following detailed description of preferred embodiments when consideredin connection with the appended drawing in which:

FIG. I shows a pyrolysis apparatus of the invention in side elevation, and partly in section; and

FIG. 2 shows a modified element for use in the apparatus of FIG. 1.

Referring initially to FIG. 1, there is seen a sectional tower whose topmost element is a combustion chamber 1 flanged to a Venturi mixer 2. The latter is mounted atop an-upright tubular vessel 3 whose cavity is divided by a coaxial, cylindrical wall 4 of porous material into a central reaction chamber 5 and an annular pressure chamber 15. The bottom section of the tower which supports the vessel 3, the mixer 2, and the combustion f chamber 1, is a cooling chamber 6 having a wide outlet 7 in its curved vertical wall. The chambers l, S and 6 and the diverging converging passage of the mixer 2 jointly form a straight vertical conduit.

The otherwise closed top wall of the combustion chamber 1 is separately supplied with fuel and oxygen through supply lines 8,9, and the length of the flame and the temperature of the combustion gas can be controlled in a known manner by a steam inlet 10 on the lower portion of the combustion chamber near the mixer 2.

A fluid hydrocarbon raw material is admitted to the throat or mixing chamber of the Venturi mixer 2 by a pipe 11. A flanged nipple 12 on the vessel 3 admits oxygen under pressure to the chamber 15. A pipe 13 communicating with the cooling chamber 6 near the top of the latter permits a cooling fluid to be introduced into the chamber 6 above the outlet 7. The bottom flange 14 of the chamber 6 may be apertured in a conventional manner, not shown,,to permit discharge of pyrolysis products not passing through the outlet 7 and of an excess of liquid cooling fluid if employed.

It will be understood that the apparatus is further equipped with control valves in the several supply lines for proper adjustment of process variables, and with indicating or recording instruments for measuring flow rates of materials entering the illustrated apparatus and for indicating temperatures wherever of interest.

The combustion chamber 1, the mixer 2 and the cooling chamber 6 are lined with refractory material in a conventional manner. The wall 4 is made of sintered spherical particles. of phosphor bronze having a nominal composition of 92 percent copper and 8 percent tin, and a solidus temperature of 880 C. Other materials which have been used successfully include a similar bronze wall prepared by sintering short length of wire, walls of sintered nickel and stainless steel, and sintered ceramic materials such as alumina, zirconia, mullite or cermets consisting mainly of alumina or chromium oxide and Cr, Mo, Co, W as the metallic constituent. It is preferred to prepare the porous wall 4 by sintering, but other methods of construction may be resorted to.

Hydrogen or a gas rich in hydrogen content is the preferred fuel which is admitted to the combustion chamber 1 through the supply line 8. It is burned with a stoichiometrically equivalent amount of oxygen discharged from the line 9. The gaseous residue recovered from the work-up of the pyrolysis products is usually a suitable fuel and may be recycled to the combustion chamber I. Any gas containing elementary oxygen may be employed for combustion if commercially pure oxygen is not available or if the resulting dilution of the product is acceptable. Atmospheric air or air enriched with oxygen may thus be employed.

The temperature of the combustion gas is close to 2,000 C. and may be adjusted by introducing steam through the inlet 10, thereby also controlling the length ofthe flame emanating from the lines 8,9.

The hotgas is mixed in the throat of the Venturi 2 with the hydrocarbon raw material that is to be pyrolyzed and which is initially in the liquid state. The temperature of the hydrocarbons is raised almost instantaneously to the desired pyrolysis temperature by suitable control of the feed rates. Typically, the reaction temperature is 750 C. for the preparation of propylene and ethylene as the predominant pyrolysis products, and somewhat higher if it is desired to prepare mainly ethylene and acetylene, the necessary conditions for pyrolysis being well known among those skilled in the art and not different in the method of this invention from the usual operating conditions.

The period during which the raw material is heated through the temperature range below the pyrolysis temperature is extremely short, and the percentage of undesired products known to be generated at the lower temperatures by polymerization, dehydrogenation or cracking is minimal. It is further reduced if the temperature in the reaction chamber is controlled to rise in the direction of fluid flow.

Thermal energy is supplied to the stream of material in the chamber 5 by partial combustion of the pyrolysis products by feeding an amount of secondary oxygen supplied through the porous wall 4 from the pressure chamber 15. Hydrogen, methane and carbon monoxide in the mixture are preferentially oxidized to maintain the initial pyrolysis temperature, or to raise the temperature of the gaseous stream for further pyrolysis of compounds of relatively high molecular weight formed in the initial stage of pyrolysis.

The additional oxygen or oxygen bearing gas employed in the secondary combustion enters the pressure chamber 15 through inlet 12 at relatively low temperature, and thus protects the wall 4 against the high temperatures prevailing elsewhere in the reaction chamber 5. The flow of gas through the pores of the wall 4 is rapid enough to prevent the deposition of carbon on the inner wall surface which would impede further entry of secondary oxygen.

The reaction mixture is quickly cooled in the chamber 6, typically to about 500 C., by'a fluid coolant introduced through the pipe 13. Any suitable and available process fluid may be employed as coolant, and it may be liquid or gaseous. Water in the liquid form or as steam may be employed, but liquid or gaseous hydrocarbons have also been employed. An excess of liquid coolant, if any, is withdrawn through the bottom flange 14 whereas the gaseous pyrolysis products together with combustion products and volatile coolant are withdrawn from the illustrated apparatus through the outlet 7 for recovery of thermal energy and fractionation in a conventional manner.

The temperature in the several axial zones of the reaction chamber 5 may be controlled more precisely by axially dividing the pressure chamber 15 and byindividually .controlling the admission of oxygen to the compartments so formed. FIG. 2 illustrates a different method of controlling the temperature distribution in a combustion chamber 5' radially bounded by a porous wall 4' which flares conically in a direction from the Venturi mixer 2 toward the cooling chamber 6. The mixer and cooling chamber are not shown in FIG. 2,

'and it will be understood that the apparatus of FIG. 2 is identical with that illustrated in FIG. I as far as not specifically shown in the drawing.

Because of the conical shape of the wall 4', its permeability to oxygen entering from the pressure chamber 15 through an axial unit length of the wall increases in a direction away from the combustion chamber 1. Conversely, the ultimate flow rate of the pyrolysis mixture in the chamber 5' is lower than in the cylindrical chamber 5 if the initial flow rate was the same. It is therefore easier to maintain an increasing temperature in the flowing pyrolysis mixture in the chamber 5 than in the chamber 5.

Obviously, the shape of the reaction chamber in the pyrolysis chamber of the invention may be modified otherwise to adapt it to specific processing conditions. It has been found, however, that one of the advantages of the apparatus illustrated is its great versatility, and its ability to operate successfully over the entire range of conditions normally required for pyrolysis of hydrocarbon raw materials to compounds having shorter carbon chains, more specifically lower alkenes and lower alkynes.

The following examples are further illustrative of the method of invention as performed in apparatus of the type illustrated:

EXAMPLE 1 A laboratory reactor of the type shown in FIG. 1 was used for pyrolysis of a gasoline fraction boiling between 80 C and 180 C. The porous wall 4 of the reactor had an internal diameter of 40 mm, and other dimensions of the combustion chamber 1, the Venturi mixer 2, and the vessel 3 may be read from the drawing which is substantially to scale with respect to elements 1, 2, 3, 4.

The gasoline entered the mixer 2 through the pipe I l at a rate of 5 kg per hour and a temperature of 500 C. For each kilogram of raw hydrocarbon stock, the combustion chamber was supplied with 0.415 cubic meter of a fuel gas consisting of 42 percent hydrogen, 38 percent carbon monoxide, and 20 percent methane, and having a net heating value of 4.792 Cal.per m. It will be understood that all percentage values are by volume unless stated otherwise, and that absolute values of gas volume relate to measurements reduced to standard conditions of temperature and pressure.

Oxygen was supplied to the combustion chamber 1 at a rate of 0.440 m and to the pressure chamber at a rate of 0.140 m per kg of hydrocarbon stock. The dwell time of the reaction mixture in the tube 4 was 0.01 to 0.001 seconds, and the temperature in the tube had an average value of approximately 1,000 to 1,100 C., and increased by about 200 C., in the direction of gas flow. The pressure in the tube 4 was approximately 7 PSIG and the pressure differential across the wall 4 i was approximately mm Hg.

The effluent gas contained, on a dry basis, 20.7 percent ethylene, 3.9 percent acetylene, 4.5 percent propylene, and 28.9 percent hydrogen, the remainder being carbon monoxide, carbon dioxide, methane and and well defined function. The fuel and primary oxygen initially fed into the chamber 1 creates a combustion media serving to generate the required level of heat for proper pyrolysis of an independent source of raw material feed. The major hydrocarbon feed, on the other hand, serves merely as the source of raw material for the production of the desired chemical end products. Thus, the raw material is distinct from the fuel and, unlike the fuel, does not become a combustion media, but the combustile which itself reacts when merely brought to the reaction temperature. It will, of course, be appreciated that the fuel and raw material, while perhaps similar in nature, are not necessmaller amounts of ethane, propane and butane. The

material recovered by condensation per kilogram of raw gasoline feed consisted of 0.41 8 kg ethylene, 0.074 acetylene and 0.139 propylene.

EXAMPLE 2 The reactor of Example 1 was supplied with the same gasoline fraction at a rate of 5 kg per hour. The combustion chamber was supplied, per kilogram of hydrocarbon stock, with 0.480 m fuel gas and 0.510 m oxygen while 0.162 m oxygen were fed to the pressure chamber 15.

The temperature in the tube 4 varied from 1,500 C. near the Venturi mixer 2 to 1,700 C. near the cooling chamber 6. The dwell time in the pyrolysis zone was approximately 0.001 to 0.0001 second and the pressure about 7 PSIG. The pressure differential across the porous wall was 25 mg Hg.

For each kilogram of gasoline fed to the reactor, 0.24 kg ethylene and 0.23 kg acetylene were recovered, the remainder of the reaction products consisting essentially, in the order of decreasing quantities, of hydrogen, carbon monoxide, carbon dioxide, methane, ethane, propane and butane.

The effect of higher operating temperature on the average chain length of the pyrolysis product is evident. Other variations in the operating conditions of the reactor may obviously be resorted to, and their results are predictable.

It is quite clear from the foregoing that each of the elements and each of the steps have their own specific sarily the same hydrocarbon materials. In fact, only some hydrocarbons may be suitable for reaction and therefore for use as a raw material.

The initial combustion of the raw material produces a primary reaction in which the hydrocarbon feed breaks down into themajor component of fluid desirable products such as the acetylene, ethylene and light hydrocarbons. However, the primary reaction leaves a residue of contaminant material such as soot, tar, etc. which would otherwise contaminate the reaction chamber and lower the performance, efficiency and rate of return of the process. This drawback and defect is overcome in accordance with the present invention by the addition of a secondary oxygen to the reaction chamber, after the raw material has been mixed with the combustion media.

The secondary oxygen fed additionally to the pressure chamber 15 is independent of either the combustion media or the raw material feed. Firstly, the secondary oxygen is fed after the fuel is combusted in chamber 1 and after the hydrocarbon raw material reaches its reaction temperature and consequently has cracked into its pyrolysis components of fluid ethylene, acetylene and lighter components as well as the unwanted contaminating products of tar, soot, coke and hydrogen. The secondary oxygen reacts with an acts to combust only these undesired contaminants and not the desired end product.

The secondary oxygen, as seen above, is supplied in quantities much smaller than the oxygen supplied for the combustion media. The primary oxygen, in fact, comprises the major portion of oxygen used.

The use of a secondary source and supply of oxygen, fed to the already reacted pyrolysis mixture, in the pressure chamber has a number of distinct advantages. Since the secondary oxygen is fed under pressure, it is uniformly distributed in the pressure chamber 15 so that it surrounds the reaction chamber and diffuses through its permeable walls. As it passes through the walls, the oxygen acts to mechanically cleanse the pores of the permeable wall of the contaminant maintaining the reactor chamber 5 clean. The secondary oxygen liquifles and thoroughly consumes the contaminant component, thus also chemically removing the tars, soot, etc.

Accordingly, the use of the secondary oxygen has succeeded in providing improved pyrolysis system with control temperature and resulting in greater efficiency and yield.

We claim:

1. A method of cracking a hydrocarbon raw material to form unsaturated hydrocarbons having a smaller number of carbon atoms which comprises sequentially:

a. burning a stream of fuel with oxygen to produce a stream of hot combustion gas;

b. mixing said stream of combustion gas with a stream of said raw material at a rate sufficient to raise the temperature of the mixture so produced to the pyrolyzing temperature of said raw material;

. introducing and passing said mixture into and e. continuously withdrawing the remainder of said products from said conduit.

2. The method according to claim 1 wherein the fuel is independent of said raw material and said additional oxygen is independent of said oxygen of the combustion gas.

3. The method according to claim 2 wherein the amount of said oxygen burned with said fuel is substantially greater than the amount of oxygen introduced through said porous wall.

4. The method according to claim 3 wherein said additional oxygen is introduced under pressure through said porous wall.

5. The method according to claim 3 wherein said initial combustion, reaction and removal of contaminant is accomplished along an axial aligned path.

6. The method according to claim 4 including the step of cooling the discharge of said product after the oxidation of said contaminant portion.

Claims

2. The method according to claim 1 wherein the fuel is independent of said raw material and said additional oxygen is independent of said oxygen of the combustion gas.
3. The method according to claim 2 wherein the amount of said oxygen burned with said fuel is substantially greater than the amount of oxygen introduced through said porous wall.
4. The method according to claim 3 wherein said additional oxygen is introduced under pressure through said porous wall.
5. The method according to claim 3 wherein said initial combustion, reaction and removal of contaminant is accomplished along an axial aligned path.
6. The method according to claim 4 including the step of cooling the discharge of said product after the oxidation of said contaminant portion.