Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
  • C07C5/42—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor
  • C07C5/48—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
  • B01J8/0285—Heating or cooling the reactor
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
  • C07C29/48—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups
  • C07C29/50—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups with molecular oxygen only
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
  • C07C41/01—Preparation of ethers
  • C07C41/05—Preparation of ethers by addition of compounds to unsaturated compounds
  • C07C41/06—Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/00106—Controlling the temperature by indirect heat exchange
  • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
  • B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/00389—Controlling the temperature using electric heating or cooling elements
  • B01J2208/00415—Controlling the temperature using electric heating or cooling elements electric resistance heaters
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00716—Means for reactor start-up
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00002—Chemical plants
  • B01J2219/00004—Scale aspects
  • B01J2219/00006—Large-scale industrial plants
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/10—Process efficiency

Definitions

• the invention is in the field of partial oxidation of hydrocarbonaceous gases.
• Partial oxidation processes both in the gaseous and in the liquid phases, have been known in the art for many years. It has long been known, for example, that methane may be partially oxidized to formaldehyde at low pressures (near atmospheric pressure), and that a substantial conversion of methane to methanol, as well as formaldehyde, occurs at elevated pressures, usually between about 50 and about 200 atmospheres.
• elevated pressures usually between about 50 and about 200 atmospheres.
• Still other problems involve preheating, maintaining and controlling the reaction temperature, and usefully recovering the substantial heat produced by the partial oxidation reaction, particularly since very large amounts of gases must be heated and reacted in comparison to the amount of product produced.
• Another object of the invention is to provide a commerciall practicable means for partially oxidizing methane and recovering in maximum ultimate yield methanol, wherein the undesired partial oxidization products are at least in part recycled, thereby both contributing to the yield of methanol and stabilizing the reaction system.
• Another general object of the invention is to provide a system for partial oxidation wherein the yield of alcohols is maximized relative to the yield of aldehydes and acids, wherein pressures greater than about 20 atmospheres are practicably utilized, premature reaction is inhibited, short reaction times (less than about 1 second) are practicable, and the reacted mixture - - in large volumes - - is rapidly quenched.
• Another object of the invention is to provide an economical means, by partial oxidation of hydrocarbons higher than methane, for the production of olefins in high yield, wherein oxygen and its reaction intermediates efficiently removes hydrogen atoms from the hydrocarbon precursor to the olefin, and wherein pyrolysis to products of lower carbon atoms is minimized.
• Another object of the invention is to provide a highly economical means for simultaneously in the same equipment producing and then combining carbinols and isobutylene to form tert-butyl ethers, wherein the ultimate yield of each of these intermediates from its precursor is enhanced relative to its production separately.
• a mixture comprising hydrocarbonaceous gases and oxygen is rapidly preheated by heat exchange with product gases from the partial oxidation reaction, then allowed to react under controlled conditions, and finally quenched by again passing rapidly in heat exchange.
• the mol ratio of hydrocarbon to oxygen is maintained above about 8 and the heat exchanger is a compartmented, radial flow rotary regenerator, the matrix of which is comprised of inert fibers of ceramic in glassy form, which inhibit undesired reactions during preheat and quench.
• the reaction space is preferably size-controllable and the speed of rotation of the regenerator is varied to control the preheat of the reactant gases.
• the annular matrix of the regenerator is readily fabricated, compartmented and strengthened by winding glassy ceramic cloth on a core and forming a line of ceramic cement across the face, rotating the core by a fraction of a revolution, and repeating.
• the rotating matrix is fitted with inner and outer rotating plenum means for distribution Of the gases across the face of the matrix and collecting the gases therefrom, and leakage of reactant gases into product gas is minimized by providing seal shoes which are self-adjusting towards the containing walls of the plenum, by causing each shoe to move toward the cooperating wall under the action of a biasing force, while a small clearance is maintained between the shoe and the wall by injecting a small flow of a relatively high pressure fluid between them.
• the configuration of the increments of reactant gas entering the reaction space in the preferred embodiment is such that homogeneity of reaction is obtained, by providing a sufficient induction time and temperature for the first increment while later, less preheated, increments are "seeded" with free radicals by the first increment, and, at the same time, the first increment is prevented in overshooting in temperature by the later, cooler increments admixed therewith.
• This preferred configuration also permits advantageously short residence times for the bulk reaction, while providing sufficient induction time for the generation of the necessary free radicals which cause the partial oxidation. Accordingly, the partial oxidation reaction is stabilized at the optimum conditions.
• methyl tert-butyl is directly synthesized from methane and isobutane by simultaneous partial oxidation to methanol and isobutylene, respectively; removal of water from the reaction gas; and then combination of them over an acid-reacting solid catalyst.
• Figure 1 is a schematic diagram illustrating the preferred method and apparatus of the invention for producing and then combining ⁇ arbin ⁇ ls and isobutylene to produce tert-butyl-ethers, sometimes referred to hereinafter as the "Metherox" process
• Figure 2 is a diagrammatic view in plan of a horizontal section of the preferred, rotary heat exchanger-reactor of the invention, sometimes referred to hereinafter as a "methanoxer", in which the reactant gases are quickly preheated, reacted, and quenched and cooled
• Figure 3 is a diagrammatic side elevational view illustrating the preferred method of the invention for constructing and compartmenting the preferred ceramic fiber rotary heat exchange matrix of the methanoxer
• Figure 4 is a diagrammatic side elevational view illustrating an indexing system for stepped rotational movement in Figure 3.
• the Metherox Process Figure 1 illustrates diagrammatically the preferred steps of a preferred embodiment utilizing the invention.
• relatively pure oxygen in line 10 - - compressed to at least reaction pressure which is preferably between about 20 and about 200 atmospheres absolute (ata), and usually between about 50 and about 100 ata - - is mixed with recycle gas delivered by blower 11 and fresh hydrocarbonaceous feed in line 12.
• reaction pressure which is preferably between about 20 and about 200 atmospheres absolute (ata)
• this feed would comprise methane (and for higher alcohols, the corresponding hydrocarbon).
• isobutane is fed along with methane.
• the reaction mixture in the latter case comprises both a relatively high ratio of hydrocarbon to oxygen (always beyond the rich explosive limit, preferably greater than 4, and more preferably greater than about 8, and for economic reasons, less than about 40, mols of hydrocarbon per mol of oxygen); and a relatively high ratio of methane to isobutane, again preferably greater than 4, and more preferably greater than about 8 mols of methane per mol of isobutane.
• the reaction mixture is preheated, preferably by the rotating ceramic fiber matrix 15, which is rotated by motor 16 and shaft 17 at between about 1 and about 20 revolutions per minute (RPM), and usually between about 5 and about 15 RPM.
• the matrix is preferably compartmented and constructed as described by reference to Figure 3, preferably comprising inert inorganic oxides combined in a glassy form and woven into a cloth from continuous filaments.
• the precise composition of the ceramic is not critical to the desired reaction (provided that it is commercially "low” in easily reducible oxides such as those of iron) and thus can be selected from materials, generally available commercially, based upon the necessary temperature resistance required.
• reaction outlet temperature is preferably between about 450°C. and about 700°C., more preferably between about 550oC. and about 650°C.
• preheat temperature is preferably between about 425°C. and about 600°C., and will usually average between about 475°C. and about 550°C.
• reaction zone 18 After reaction in reaction zone 18 the product gases pass back through another portion of matrix 15. During reaction the temperature of the gases increases substantially due to the exothermic nature of the reaction so that then the gases are hotter than the solids in the matrix, and serve to heat it as they are being cooled. Thus is a temperature gradient established in matrix 15. And thus this quench rate, generally of over 1000°C./second, combined with the large surface area, effectively quenches the secondary, undesired reactions.
• Heat is further usefully recovered from these gases in line 19 by their serving to provide heat in necessary reboil duty in other steps in the process, as indicated by heat exchange loops 20, 21, 22, 23 (supplemented where or if necessary by steam or other hot medial . During this further cooling, water vapor and some methanol will generally condense, further recovering (latent), heat.
• the temperature at the top of vessel 25 may be adjusted so that the net make of the various products and byproducts, comprising formaldehyde and isobutanol, is carried overhead into line 34, along with the gases introduced to vessel 25 via line 32; or alternatively a small liquid stream (not shown) may be taken from line 31 and passed directly to the catalytic reaction zone 33 of vessel 14; or, if desired, this minor product may be separately removed from the system.
• a substantial portion of the methanol product will also pass overhead as vapor in line 34, while essentially all of the water vapor in the gases in line 32 is absorbed therefrom by the (dried) liquid entering vessel 25 via line 31.
• This water-enriched liquid will then pass via line 35, backpressure valve 36, exchanger 29, and line 37 to water stripper vessel 26.
• the overhead from this stripper in line 38 will comprise a complex mixture, including. some fixed gases which are vented via Line 39 after condenser 40 and separator 41. Depending upon exact reaction and operating conditions, the liquid phase from condenser 40 will probably split into two phases, which is preferred. If not, a relatively very small amount of hydrocarbonaceous material, preferably that which is valuable in the final product, such as natural gasoline, naphtha, benzene, or toluene, added to the vapor in line 38 (or other adjacent convenient point) will suffice to cause this separation into two liquid phases. Since the hydrocarbonaceous phase is completely refluxed to the top of vessel 26, the added material, if any, almost entirely returning back overhead, very little makeup of such material will be required.
• the aqueous phase from separator 41 is passed to fractionator-stripper vessel 42, and comprises methanol and water. From the bottom of vessel 42 the stream 43 comprising water is removed, while a methanol fuel stream is produced from the overhead vapors in line 44, via condenser 45, separator 46 and pump 47. Depending upon the production of methanol and other carbinols relative to that of isobutylene, all or part of this methanol may be required within the process to produce tert-butyl ethers. This requirement is recycled via line 48, with the excess production being removed via line 49. Some gases also vent via line 50.
• the novel preferred system of the invention for reacting meth-mol and other carbinols with isobutylene to form tert-butyl ethers as described below uniquely overcomes some otherwise serious problems with this combination reaction.
• the reaction is inhibited by high methanol concentrations - - which methanol is preferentially imbibed by the catalyst to the exclusion of isobutylene therefrom. Also the reaction is exothermic and limited by equilibrium.
• the reaction is first inhibited by high methanol content and then, through heat release as well as tert-butyl ether formation, by equilibrium. Both the methanol concentration profile and the temperature profile during reaction thus tend to be just opposite to that desired, necessitating excessive catalyst requirements and elaborate heat exchange requirements with cooling water.
• the elaborate cooling provisions are eliminated; i.e., the entering gas can be already cooled to any desired temperature, thus cooling the tert-butyl ether product towards the end of its reaction, when it would conventionally be most limited by equilibrium.
• the preferred embodiment readily provides for recycle to the reaction zone of both isobutylene and methanol contained in the crude tert-butyl ether stream, so that equilibrium problems are obviated.
• the gases containing isobutylene and some of the product methanol entering vessel 14 via line 34 are met by downflowing liquid comprising methanol, tert- butyl ethers, and some dissolved isobutylene.
• the liquid absorbs isobutylene from the upflowing gas in zone 33 of vessel 14, and its favorable temperature - - prefereably about 40°C.-90oC. and more preferably about 50°C.-70°C - - and ratio to methanol enhances its reaction rate within the pores of the catalyst, preferably arranged in packed sections 51 above and below line 34.
• the first carbinols to accumulate in the liquid near the junction of line 34 are isobutyl alcohol and its hemiacetal referred to above. They react within the catalyst with isobutylene to. form isobutyl tert-butyl ether (TBE) and isobutoxymethyl TBE, respectively.
• the byproduct oxides mainly isobutylene oxide, also react within the catalyst in the presence of methanol first to form a glycol ether, and then, in the presence of isobutylene, to form methoxyisobutyl TBE.
• TBE's The principal use of TBE's is as a valuable antiknock in gasoline, which in the optimum 7%-10% level therein not only replaces lead antiknock compounds, but also extends the volume of gasoline, utilizing natural gas components rather than increasingly costly petroleum oil. And it is to be expected that these byproduct TBE's will have comparably high blending octane values to that of the methyl analog, MTBE, and thus be approximately equally valuable (per mole of TBE). (At the same time they may, however, require a somewhat greater amount of anti-oxidant gum- inhibitor additive) .
• the downf lowing crude tert-butyl ether product from packed sections 51 then preferably enters stripping section 52 where dissolved fixed gases are stripped therefrom, passes through line 53 and backpressure valve 54 to stabilizer vessel 55 where components boiling lower than methyl tert-butyl ether (MTBE) are at least in part stripped therefrom, to control vapor pressure of the product.
• MTBE methyl tert-butyl ether
• the offgases from section 67 preferably enter blower 11 via line 70, and most of the gases therefrom are recycled to the partial oxidation reaction.
• the excess accumulation of gases, comprising byproduct carbon monoxide as well as residual methane, is preferably taken from the discharge of. blower 11 in line 73, and passed separately by a line not shown and separately enters matrix 15, where it is. preheated, thereby recovering relatively high temperature heat therefrom, and leaves matrix 15 and vessel 14 via separate passages and line 71.
• This preheated offgas is preferably furnished to an expander 72 to recover useful energy, and may then serve to augment fuel gas or utilized in other well-known ways to recover its valuable components.
• Regenerative Preheat/Reactor Referring to Figure 2, which schematically shows in enlarged horizontal sectional view the preferred arrangement of heat exchanger/reactor 13, it is preferred that the various flows by symmetrical about the centerline.
• rotating matrix 15 is in pressure balance, inasmuch as while the only pressure differences are due to pressure drops caused by flow therethrough - - in contrast to other uses of rotary heat exchangers, such as in gas turbine regenerators - - still such differences exerted over substantial areas may unduly cause operational problems.
• Such symmetrical flows are accomplished by providing the matrix 15 with an annular arrangement of uniformly sized radial compartments 15a separated from adjacent compartments 15a by radial walls 15b that may be made of ceramic cement as described below.
• the outer seal shoes 100, 101, 102, 103, 104, 105, 106 and 107 may be separate structures mounted on the vessel wall 108 as shown, or they may be combined together in a pair of shoes opposing each other within which the entering gases are fed to the appropriate sections of matrix 15, as more fully described in my co-pending application Serial No. 228,908, the open spaces between the pair of shoes then serving as exit plenums.
• recycle gas (not containing oxygen) to flush out (inwards) oxygen-containing gas be introduced, - - via lines 109 and 110 - - to that compartment which is just before the flow within the matrix reverses, and commences flowing outward.
• recycle gas is preferably introduced into that matrix compartment which is just about to switch back to inward flow prior to its closing at the inner fixed shoes 112 and 113.
• the recycle gas first backflushes reacted gas back through the matrix, thereby causing such reacted gas to tend to exit via a prior compartment; and then this backflushing gas feeds to plenum 111 as the particular compartment reaches the openings between seal shoes 112 and 114 and between shoes 113 and 115.
• the inner plenums 116 and 117 In startup operation, in order to establish a temperature gradient in matrix 15 such that feed is sufficiently preheated so that partial oxidation can commence, the inner plenums 116 and 117 must be heated.
• the heat exchange efficiency of the rotating matrix 15 is intrinsically very high, especially at the substantially reduced flow rates preferred for startup, relatively little heat will be required since it will be almost completely recovered by being stored within the inner portions of matrix 15.
• auxiliary heater or other means can be employed, it is preferred that electrical, resistance-heated startup rods 118 and 119 be employed.
• the hot surface of these rods will relatively quickly initiate partial oxidation, the heat release from which will perform most of the heating; also these hot rods will stabilize the oxidation Before final operating temperatures are reached, as flow rates are increased.
• residence time control baffles 120 through 123 which are preferably hinged to inner shoes 112 through 115, respectively, are preferably drawn back against plates 126 and 127 containing plenum 111, thereby maximizing the reaction space available in plenums 116 and 117.
• active residence time i.e., the residence time for the bulk of the reacting gas, be held at a minimum, consistent with economic considerations of pressure drops and the like and the necessity of providing for the necessary induction period.
• Reduction of residence space is preferably accomplished by rotating the baffles 120 through 123 into a position similar to that shown, such that most of the residence space is rendered inactive, and the bulk of the gases first pass inward through the sections of the matrix between shoes 100 and 107 and between shoes 103 and 104, thereby being rapidly preheated, preferably build up in radical concentration in the space prior to the startup rods, and just complete their reaction (i.e., utilize substantially all of the oxygen available) before then being removed from the reaction zone by passing outward through the sections of matrix 15 radially between shoes 101 and 102, and between shoes 105 and 106.
• fixed baffles 124 and 125 be installed such that they first direct the last of the preheated gas into mixing in the active zone of free radical buildup just prior to the startup rods, and as shown require such gas to have at least a minimum of reaction residence time before being quenched by passing back into matrix 15. It is to be emphasized that this form of preheatreactor-quench system has unique advantages. First, it povides great stability to exothermic reaction systems and provides substantially more "isothermal" reaction kinetics than common exothermic reaction systems. Second, it combines the desirable features of plug flow with those of "cold shot" admixture and with those of backmixing.
• the first inflow i.e., excess recycle gas taken as hot offgas through plenum 111
• the first inflow will be preheated to the maximum possible temperature.
• heat is usefully recovered for use elsewhere at the highest possible temperature.
• the main point here is that the first of the next inflowing gas is also heated to a relatively high temperature. This gas then relatively quickly builds up in the necessary free radical concentrations to effectuate the desired partial oxidation.
• this first increment of reaction gas would by its heat release during reaction tend to overshoot in respect to the desired reaction temperature.
• the present invention achieves stability by the relatively long residence time of the early, hotter increments without "short-circuiting" any increments, and without “over-treating” any increments.
• the early, hotter increments are not “overtreated” because until free radical concentrations have built up in them very little bulk conversion is occurring; thus desired converted products are not substantially present, and thus are not appreciably undergoing parasitic loss.
• the effective bulk reaction zone - - as distinguished from the induction zone - - may readily be optimized to a relatively very short distance, amounting to about one-fourth of the total reaction path length.
• a very small bulk residence time is .important in order to maximize yields from such exothermic reactions where the desired products are inherently more, readily attacked than is the reactant precursor.
• Matrix Frabrication By reference to Figure 3 and Figure 4, it is shown how it is preferred to fabricate matrix 15 , to compartment it and to seal its top and bottom extremities. As mentioned in reference to Figure 1, it is preferred that the matrix be fabricated from cloth; cloth of selected porosity and thread size woven preferably from continuous filament yam of glassy ceramic composition.
• a spool of continuous cloth 200 is mounted upon a spindle shaft 201 fitted with a friction-restraining device.
• this restraining device is a small, fixed hydraulic, oil-filled motor 202, the shaft of which is attached to shaft 201, with the oil feed and discharge of motor 202 connected together through valve 203.
• the spool will turn motor 202, and will unwind slowly, at a rate dependent upon the setting of valve 203.
• Cloth 200 passes under idler roll 204, suitably supported (not shown) so that rotational and vertical, but not significant horizontal, motion is permitted.
• This idler roll by its weight provides relatively constant tension on the cloth, in spite of intermittent motion downstream from it.
• valve 203 may be readily controlled by the vertical position of idler roll 204, thereby holding the position of roll 204 within closely defined limits, and in turn holding the tension on cloth 200 virtually constant.
• the free end of cloth 200 is temporarily attached to a removable mandrel or held by a perment core 205 (used in the final matrix to collect gases at the inner periphery of matrix 15) mounted on shaft 206.
• indexing device 207 shown in Figure 4, which has a number of circumferential positions equal to the number of radial compartments into which it is desired to divide matrix 15.
• Cooperating with device 207 are, solenoid or preferebly compressed air piston-operated, stop device 208 and, solenoid or preferably compressed air piston-operated, ratchet device 209.
• Ceramic cement application "gun” 210 and its carriage (not shown) which is slidably attached to runners 211 and 212, and is preferably actuated in back and forth motion along runners 211 and 212 by a compressed air piston (not shown), or other suitable means, such as a reversing motor and attached drum driving an endless cable over pulleys located beyond either extremity of the desired traverse.
• runners 211 and 212 together with associated equipment are also mounted upon a carrier (not shown) which may be manually or automatically adjusted horizontally to maintain a desired relationship with the face of accumulating cloth 200 upon core 205.
• the "gun" carriage mounted upon runners 211 and 212 is also preferably fitted with a small compressed air piston (now shown) actuated such that when, at the end of its travel along runners 211 and 212, gun 210 is momentarily vertically tilted through a fixed arc and then returned to its horizontal position. This projected arc is at least equal to the distance between adjacent compartment barriers or walls 15b.
• additional guns may be mounted to apply ceramic cement circumferentially to the extremities of the matrix, rotational increment by increment.
• stop device 208 As soon as it reaches the end of its travel, stop device 208 is raised, ratchet device 209 activated to turn shaft 206 one notch and stop device 208 again locks the position of shaft 206; whereupon the front of the gun 210 is vertically tilted momentarily through an arc to apply cement in a direction further along the cloth to be cemented near to the extremity of the cloth 200, thereby cementing the edge of two compartments. Gun 210, back in its horizontal position, applies ceramic cement back across the face of cloth 200 to the extremity of its travel in the opposite direction. And the sequence repeats at the other end.
• TBE tert-butyl ether

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Citations (8)

• 1982
  • 1982-01-19 AU AU82009/82A patent/AU8200982A/en not_active Abandoned
  • 1982-01-19 BR BR8205841A patent/BR8205841A/pt unknown
  • 1982-01-19 JP JP57500808A patent/JPS58500128A/ja active Pending
  • 1982-01-19 EP EP19820900726 patent/EP0070304A4/en not_active Withdrawn
  • 1982-01-19 WO PCT/US1982/000061 patent/WO1982002548A1/en not_active Application Discontinuation
  • 1982-01-26 ES ES509059A patent/ES8307691A1/es not_active Expired
  • 1982-01-27 IT IT19324/82A patent/IT1190673B/it active
  • 1982-09-16 NO NO823138A patent/NO823138L/no unknown

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