Showing papers on "Partial oxidation published in 1970"

Sewage disposal process

Abstract: SEWAGE IS CONVERTED INTO A SUSEFUL NON-POLLUTING PRODUCT GAS, E.G. SYNTHESIS GAS OR FUEL GAS BY DEWATERING MUNICIPAL SANITARY SEWAGE, PRODUCING A THICKENED SLUDGE. THE THICKENED SLUDGE IS MIXED WITH A FLUID SELECTED FROM THE GROUP CONSISTING OF H20, LIQUID HYDROCARBON FUEL, PARTICULATE CARBON SLURRIES IN WATER OR IN A LIQUID HYDROCARBON FUEL IS PRODUCED SUBSEQUENTLY IN THE PROCESS, AND MIXTURES THEREOF TO PRODUCE A FEED MIXTURE STREAM. PREFERABLY THE FEED MIXTURE IS HEATED TO A TEMPERATURE IN THE RANGE OF ABOUT 212 TO 600*F. TO VAPORIZE VOLATILE CONSTITUENTS IN THE FEED MIXTURE AND TO PRODUCE A FEED DISPERSION STREAM. THE FEED DISPERSION IS THEN REACTED BY PARTIAL OXIDATION WITH AN OXYGEN-RICH GAS IN AN UNPACKED FREE-FLOW NON-CATALYTIC SYNTHESIS GAS GENERATOR, AT A TEMPERATURE IN THE RANGE OF ABOUT 1500 TO 3000*F. AND AT A PRESSURE IN THE RANGE OF ABOUT 1 TO 250 ATMOSPHERES TO PRODUCE SYNTHESIS GAS. WATER SEPARATED FROM THE SEWAGE IS PURIFIED AND USED FOR INDUSTRIAL APPLICATIONS OR CONVERTED INTO BY-PRODUCT STEAM BY INDIRECT HEAT EXCHANGE WITH THE PRODUCT GAS. IN A SECOND EMBODIMENT OF THE INVENTION, GARBAGE IS DISPOSED OF BY MIXING BITS OF GARBAGE WITH THICKENED SEWAGE SLUDGE AND THE AFORESAID FLUID THEREBY FORMING A FEED MIXTURE WHICH IS CONVERTED INTO SYNTHESIS GAS BY THE PARTIAL OXIDATION REACTION WITH AN OXYGEN-RICH GAS IN SAID FLOW TYPE GAS GENERATOR. D R A W I N G

A Study of the Partial Catalytic Oxidation of Hydrocarbons. V. The Effect of Phosphorus Addition to the Vanadium Catalyst on the Oxidation of Butene, Butadiene, and Furan

Abstract: In the present investigation, the vapor-phase partial oxidation of cis-2-butene, butadiene, and furan was carried out over V2O5 and V2O5-P2O5, (1 : 1.6 atomic ratio), with various contact times, at 350°C, and at the concentration of 0.6–1.6% in air, in order to elucidate the effect of phosphorus addition to V2O5, on the selectivity and mechanism of butene oxidation. Oxidation activity decreased remarkably with an increase in the phosphorus content. In the presence of phosphorus (P/V=1.6), selectivity for the C4H8→C4H6 step and C4H6→C4H4O step were considerably increased, from 46 to 88 and from 72 to 93 mol% respectively, while selectivity for the C4H4O→maleic anhydride (MA) step fell from 60 to 50 mol%, due to the increase in polymer formation. From the results, it was concluded that V2O5 and V2O5-P2O5 catalysts show similar oxidation activity with regard to butene, butadiene, and furan, and that the quantities of the intermediate products are fairly much affected by the activity of the catalyst as well a...

Exhaust gas treatment system

Abstract: An exhaust gas treatment method and system for an internal combustion engine utilizing a catalytic converter, wherein carbon or charcoal is incorporated into the system so that the gases H2 and CO can be produced by the dissociation of water, present in the exhaust gas, and the partial oxidation of the carbon to become a secondary fuel for a catalytic conversion zone of the converter. In a preferred embodiment at least a portion of the exhaust gases are caused to pass through a bed of carbon under predetermined conditions prior to their entry into the catalytic converter intermediate between engine startup and a predetermined high limit temperature.

Oxidation of ethylene at a palladium electrode

Abstract: The electrochemical oxidation of ethylene to acetaldehyde and carbon dioxide is investigated at a palladium electrode in 2 N sulphuric acid at 80°C, as a first step towards the partial oxidation of higher olefins. Results on the corrosion of a palladium electrode in the absence of ethylene show features not previously reported, and a possible mechanism is given to account for the results. In the presence of ethylene at electrode potentials above 0.75 V EH, it is shown that two reaction schemes are likely to be in operation to account for the products observed, as well as the appearance of a considerable amount of palladium metal in the electrolyte.

Production of a methane-rich synthesis gas

Abstract: Methane-rich synthesis gas comprising H2, CO, CO2 and 10 to 26 percent by volume of CH4 (dry basis) is produced by the partial oxidation of a hydrocarbonaceous fuel in a free flow noncatalytic synthesis gas generator at a reaction temperature below 1,700 DEG F., a pressure in the range of about 15 to 250 atmospheres, and a steam of fuel weight ratio in the range of about 3 to 5. The product gas, after removal of CO2 and H2S has a heating value in excess of 400 BTU/SCF.

Improvements relating to the Production of Ammonia

Abstract: 1,186,939. Ammonia production. WHESSOE Ltd. 4. Sept., 1968 [8 Sept., 1967; 11 Oct., 1967; 15 Feb., 1968; 20 March, 1968], Nos. 41233/67, 46463/67, 7553/68 and 13527/68. Heading C1A. Ammonia is produced by catalytic conversion of an N2/H2 synthesis gas mixture, the hydrogen being- produced by the reforming and/or partial oxidation of one or more hydrocarbons with subsequent removal, of unrequired substances, wherein.the conversion is effected at the same, or higher, pressure as the synthesis gas is produced, the conversion being at 600-1000 p.s.i.g. in a converter, the inlet temperature of which is kept low enough to ensure that. the exothermic reaction does not cause a temperature rise emough to damage the catalyst, and the removal of NH3 being-at-leastpartly by absorption. or adsorption.. By operation, at low pressures, the low yield (e.g. 1%), is compensated by simplicity of operation and apparatus. The synthesis gas is preferably recycled after NH3-recovery. The recovery may be by absorption in a liquid, e.g. water, H2SO4, HNO3, or by adsorptionon active carbon or on a molecular sieve; or by refrigeration. The NH3 may be recovered from water by pressure distillation.

Method and apparatus for soot controlling in a thermal decomposition of a hydrocarbon gas

Abstract: FORMATION OF SOOT WHEN A HYDROCARBON GAS IS THERMALLY DECOMPOSED WITH AIR BY PARTIAL OXIDATION IN AN ENDOTHERMIC GAS GENERATOR FILLED WITH AN OXIDATION CATALYST LAYER, CAN BE CONTROLLED BY INTRODUCING A FEED GAS MIXTURE OF THE HYDROCARBON GAS AND AIR RAPIDLY AND ADIABATICALLY, WITHOUT ANY STAGNATION OF GAS FLOW, INTO A CATALYST-FILLED RETORT MAINTAINED AT A RETORT TEMPERATURE OF 1,000* TO 1,000*C. BY HEATING FROM OUTSIDE THROUGH A PERFORATED HEAT-INSULATING BLOCK HAVING A THICKNESS ENOUGH TO ATTAIN A HEAT INSULATION AND THERMALLY DECOMPOSING THE HYDROCARBON GAS IN THE CATALYST LAYER, WHILE SUPPLYING HEAT TO THE CATALYST LAYER FROM THE OUTSIDE HEATING SOURCE. THE HEAT-INSULATING BLOCK COMPRISES A HEAT-INSULATING BRICK AND A REFRACTORY BRICK AND IS PLACED DIRECTLY UPON THE CATALYST LAYER WITHOUT ANY CLEARANCE THEREBETWEEN. BY PROVIDING THE HEAT-INSULATING BLOCK IN THE GENERATOR, OPERATION OF THE GENERATOR CAN BE CARRIED OUT STABLY FOR A PROLONGED PERIOD OF TIME WITH A CONSTANT GENERATED GAS COMPOSITION.

Catalytic Activity of Vanadium-Molybdenum Oxide Catalysts in Partial Oxidation of Budadiene

Abstract: V2O5 および V2O5-MoO3 系触媒を用いて, ブタジエン, フラン, クロトンアルデヒドの接触空気酸化を, 350℃, 空気過剰のもとで行ない, V-Mo 組成の変化による, ブタジエン酸化の活性, 選択性および反応機構におよぼす効果を検討した。V2O5-MoO3 触媒のブタジエンなどの酸化活性は, Mo 含量 20 atom% 付近が最大であり, ブタジエン, フラン, クロトンアルデヒドの反応性は, ほぼ同じ程度であった。ブタジエン酸化の中間生成物であるフラン, クロトンアルデヒド生成量は, V-Mo 組成によらず, ブタジエン反応率約 50% 付近に頂点をもつ山型となり, V-P 系触媒にくらべ, フランの生成量は 1/3 程度で, またフランの約 1/2 のクロトンアルデヒドの生成がみられた。無水マレイン酸への選択率は, ブタジエンからは, V2O5 触媒で 43%, V2O5-MoO3 (Mo/V>1/2) で 53%, フランからは, V2O5 で 60%, V2O5-MoO3 で 73% であった。Mo 添加により, ブタジエンから無水マレイン酸への選択率が増加するのは, ブタジエンからフランへの段階が影響されたのではなく, フラン以後の段階の選択性が高められたためと考えられる。

Catalyst for hydrocarbon oxidation

Abstract: A CATALYST USEFUL FOR THE OXIDATION OF ORGANIC COMPOUNDS, PARTICULARLY THE PARTIAL OXIDATION OF BENZENE WITH MOLECULAR OXYGEN TO PRODUCE MALEIC ANHYDRIDE, COMPRISES THE OXIDES OF MOLYBENUM AND VANADIUM AND A MINOR AMOUNT OF BORON. A PREFERRED FORM OF THE CATALYST FURTHER INCLUDES PHOSPHORUS AND AT LEAST ONE MEMBER OF THE GROUP CONSISTING OF COBALT, NICKEL AND IRON, AND SODIUM.

Steam reforming hydrocarbons

Abstract: 1,200,448. Making combustible gas. IMPERIAL CHEMICAL INDUSTRIES Ltd. 3 Oct., 1967 [10 Oct., 1966], No. 45204/66. Heading C5E. A hydrocarbon feedstock of high C.V. and high hydrogen to carbon ratio is catalytically steam reformed in substantially non-oxidative conditions to give a gas containing H 2 and carbon oxides, and the gas is catalytically partially oxidized with O 2 (air) to produce a gas of lower C.V. and lower hydrogen to carbon ratio. There is sufficient hydrocarbon present in the second (partial oxidation), step to take up by reaction with steam a substantial part of the heat evolved by the partial oxidation, so that the temperature of the gas leaving the second step is less than that of the gas leaving the first (primary reforming) step. The feedstock may be natural gas or refinery gas, and may be additionally injected between the two steps, e.g. to the extent of 25 to 60% of the hydrocarbon in the second step, permitting primary reforming at temperatures of 700‹ to 850‹ C. Methanol may be injected into one or both steps, and the second step is preferably carried out at such a temperature that carbon monoxide conversion occurs, and steam may be added to this step for this purpose. Steam ratios (moles steam per carbon atom in the feed) in the range 1A3 to 5A5, preferably 2 to 4, ensure sufficient steam for reaction with hydrocarbon in the second step. Outlet gas temperatures from the second step of 600‹ to 750‹ C. are mentioned.

Method for converting copper

Abstract: A METHOD FOR REMOVING ANTIMONY FROM A MATERIAL WHICH COMPRISES AT LEAST ONE OF THE SUBSTANCES COPPER AND COPPER SULPHIDE. OXIDIZABLE IRON OR OXIDIZABLE IRON COMPOUNDS ARE ADDED TO THE MATERIAL WHILE THIS IS IN A MOLTEN CONDITION, THE SAID OXIDIZABLE IRON OR COMPOUND BEING OF A TYPE WHICH ARE SOLUBLE IN MOLTEN COPPER OR COPPER SULPHIDE AND WHICH HAVE A LOW ANTIMONY CONTENT. THE DISSOLVED IRON IS THEN ISOLATED FROM THE MELT BY A PARTIAL OXIDATION PROCESS, SIMULTANEOUSLY OXIDIZING ANTIMONY AND BINDING THE SAME TO THE IRON OXIDE.

Process for the Production of Synthesis Gas.

Abstract: 1,193,202. Making fuel gas. TEXACO DEVELOPMENT CORP. 2 May, 1967, No. 20285/67. Heading C5E. [Also in Division C1] Hydrogen is produced by (i) subjecting hydrocarbon liquid or vapour, steam and oxygen of at least 95 vol. per cent purity to partial oxidation in an unpacked reaction zone at above 1500 p.s.i.g. and under an autogenous temperature of 2200-2800‹ F., (ii) quenching the effluent with water, at reaction zone pressure and preheated to the equilibrium temperature of the quench zone, in amount greater than that vaporizable by said effluent, (iii) subjecting the resultant mixture to a catalytic water gas shift reaction at reaction zone pressure and (iv) recovering hydrogen. Oxygen may be supplied in amount 11A7-14A4 scf. per Ib. hydrocarbon, and steam in amount 1 lb. per 1-4 lbs. hydrocarbon, to the oxidation zone which may operate at up to 5000 p.s.i.g. The quench water may be preheated to 535‹ F. for a pressure of 1500 p.s.i.g. and unvaporized quench water may be treated for removal of entrained carbon produced in the reaction zone, and recycled. The effluent gas from the quench system may be preheated by the outlet gas from the shift reaction zone prior to undergoing the shift reaction. After removal of other gases and impurities, the hydrogen may be washed with liquid nitrogen. Liquefaction and rectification of air may provide oxygen for the reaction and nitrogen for washing. Reference has been directed by the Comptroller to Specification 837,030.

Partial oxidation of hydrocarbons

Abstract: 1,210,673 Partial oxidation of hydrocarbons HALCON INTERNATIONAL Inc 20 Nov, 1967 [23 Nov, 1966], No 52594/67 Heading C2C Oxygenated compounds including alcohols and ketones are produced in the continuous molecular oxygen oxidation of at least one saturated hydrocarbon supplied as a feed containing more than 95 molar per cent saturated hydrocarbons, wherein the hydrocarbon and molecular oxygen are reacted in the liquid phase in a plurality of separate oxidation satages, connected in series, in the presence of a boron adjuvant, wherein the amount of boron adjuvant present in the effluent from the first oxidation stage is sufficient to provide at least one gm atom boron/three gm moles of total hydrocarbon alcohol (defined as consisting of the mixture of hydrocarbon alcohol as such or in the form of the hydroperoxide and the borate esters of the hydrocarbon alcohol) in said effluent but less than an amount sufficient to result in the formation of a separate solids phase in said effluent and wherein additional boron adjuvant is added to at least one other of the oxidation stages, the total amount of boron adjuvant employed in the oxidation being sufficient to provide at least one gram atom of boron per three gram moles of total hydrocarbon alcohol in the effluent from the last of the oxidation stages The product alcohols are liberated by the hydrolysis of the reaction mixture Examples use cyclohexane, cyclododecane and a C 12-14 paraffinic petroleum naphtha