CA1094612A - Dense-phase feeder method - Google Patents
Dense-phase feeder methodInfo
- Publication number
- CA1094612A CA1094612A CA298,592A CA298592A CA1094612A CA 1094612 A CA1094612 A CA 1094612A CA 298592 A CA298592 A CA 298592A CA 1094612 A CA1094612 A CA 1094612A
- Authority
- CA
- Canada
- Prior art keywords
- feeder
- vessel
- coal
- solids
- dense
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 238000000034 method Methods 0.000 title claims abstract description 13
- 239000007787 solid Substances 0.000 claims abstract description 39
- 239000007789 gas Substances 0.000 claims description 24
- 239000012159 carrier gas Substances 0.000 claims description 8
- 238000007789 sealing Methods 0.000 claims description 2
- 239000002245 particle Substances 0.000 abstract description 17
- 239000011236 particulate material Substances 0.000 abstract description 5
- 239000000463 material Substances 0.000 abstract description 2
- 230000032258 transport Effects 0.000 abstract 2
- 239000013618 particulate matter Substances 0.000 abstract 1
- 239000003245 coal Substances 0.000 description 80
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 14
- 239000001257 hydrogen Substances 0.000 description 14
- 229910052739 hydrogen Inorganic materials 0.000 description 14
- 150000002500 ions Chemical class 0.000 description 8
- 239000003463 adsorbent Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000008187 granular material Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 4
- 238000010791 quenching Methods 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- ZKFQEACEUNWPMT-UHFFFAOYSA-N Azelnidipine Chemical compound CC(C)OC(=O)C1=C(C)NC(N)=C(C(=O)OC2CN(C2)C(C=2C=CC=CC=2)C=2C=CC=CC=2)C1C1=CC=CC([N+]([O-])=O)=C1 ZKFQEACEUNWPMT-UHFFFAOYSA-N 0.000 description 1
- 101100478173 Drosophila melanogaster spen gene Proteins 0.000 description 1
- 101100513476 Mus musculus Spen gene Proteins 0.000 description 1
- 102100026933 Myelin-associated neurite-outgrowth inhibitor Human genes 0.000 description 1
- 240000008881 Oenanthe javanica Species 0.000 description 1
- 241000212342 Sium Species 0.000 description 1
- 229950004646 azelnidipine Drugs 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 238000003754 machining Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229920000136 polysorbate Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B31/00—Charging devices
Abstract
DENSE-PHASE FEEDER METHOD
Abstract of the Disclosure A method for the dense-phase flow of particulate solids utilizes a pressurized feeder and flow splitter is disclosed which transports and equally divides particulate material at essentially the bulk density with only the gas contained in interstices of the solid particles being used to transport the particles. The feeder comprises a vessel which is pressurized, a gas source for pressurization and an outlet line with a full opening valve located immediately adjacent to the feeder. The loaded vessel containing particulate matter is pressurized, followed by opening the valve adjacent the feeder, the valve and relatively empty downstream line when flow is initiated being the key to successful operation of the dense-phase feeder. The downstream flow divider evenly distributes the dense-phase material to, for example, a multiplicity of feed passages in a multi-passage injector.
Abstract of the Disclosure A method for the dense-phase flow of particulate solids utilizes a pressurized feeder and flow splitter is disclosed which transports and equally divides particulate material at essentially the bulk density with only the gas contained in interstices of the solid particles being used to transport the particles. The feeder comprises a vessel which is pressurized, a gas source for pressurization and an outlet line with a full opening valve located immediately adjacent to the feeder. The loaded vessel containing particulate matter is pressurized, followed by opening the valve adjacent the feeder, the valve and relatively empty downstream line when flow is initiated being the key to successful operation of the dense-phase feeder. The downstream flow divider evenly distributes the dense-phase material to, for example, a multiplicity of feed passages in a multi-passage injector.
Description
Background of the Invention I. _ield of the Inven~ion This invention relates to the c021 processin~ fie1d.
More particularly, this invention relates to ~he coal fluidi~a~ion field wherein dense-phase coal is equally divided between multiple iniection passages in an injector from a single coal feed line and fed to a coal reaction chamber for hydro~enation of the coal particles hy hot hydrogen injected through the injector.
More particularly, this invention relates to ~he coal fluidi~a~ion field wherein dense-phase coal is equally divided between multiple iniection passages in an injector from a single coal feed line and fed to a coal reaction chamber for hydro~enation of the coal particles hy hot hydrogen injected through the injector.
2 Description of the Prior Art I0 The following three U. S. patents issued to C. H. 0. Berg on July 27, 1954, all en~itled "Conveyance of Granular Solids", describe a means to transport solid particles in a gaseous medium: U. S. Pat.
Nos. 2,684~868; 2,684,870 7 and 2,684,872.
Since all of the foregoing patents are closely related, a brief description of U. S. Pat. 2,684,870 will suffice to describe the closest prior art to Applicant's invention. This patent describes an improved selective adsorption process in which the granual adsorbent is conv~yed upwardly through a lift line and downwardly through an adsorption column in substantially the same condition of solids bulk density. It has been found that a conduit may be maintained with a vertically rising mass of solid granular adsorbent In which the bulk density of the solids is subs~antially the same as the bulk density of the solids when at rest as static bulk density.
This is accomplished by forcing a flow of lift gas upward1y through the interstices of the granules to establish frictional forces (indicated by the pressure differential) wh;ch ar~ sufficient to overcome the gravitational ~, .. .
~3~ 76R25/77Rl2 forces on the adsorbent granules as well as the frictional forces oF the con-duit walls on the moving bed of adsorbent and cause the mass to move upward.
The actual veloclty of the lift gas necessary ~o accompllsh this result is de pendent upon the s~ze and density of the granules, and the viscosity of the lift gas which is dlrectly determin~d by the pressure and temperature. The velocities are generally su~ficient tu cause fluidization of the adsorbent granules i~ thc adsorbent granules were ~nee to fluid~ze or becDme suspended in the lift gas.
All of the Berg patents relate primarily to Yerttcal movement Df solids in a continuous Flow loop. The Berg patents~ add1tionally, describe a vertical column that has a narrow opening at the bottom of the oolu~n and a wide spen~ng at ~he top, the column describing somewhat of a cone shape. -The reason for this is to prevent clogg~ng of the column as the granules are m~ved upwardly through the pipe. Thus, it can be seen that ln the Berg referencesl clogging of the column could occur.
The present disclosure relates to a dense-phase feeding of part~culate solids through horizontal and/or vertical feed pipes. Als~ the present in-vent~vn util~zes a ~a~l valve ~mmediately adjacent to the ~eeder ~x~t t~ all~w flow of sol-~d partlcles to be established. The Berg references heretofore described initiate f10w by simply prov~ding a pressure diffPrenti~l in the vertical ~eeder line. In the present ~nventlon, if a valve positioned at the exit of the feeder vessel is not used and flow is initiated by simply pressuri-zlng the feeder vessel, the feed llne will consistently plug. In add~tion, the Berg references employ a "thrust plate" or choke at the exit of the diverging vertical tube. The present ~nvent~on does not requ~re a choke to control ~low o~ dense-phase materlal through the feeder l~nes.
Nos. 2,684~868; 2,684,870 7 and 2,684,872.
Since all of the foregoing patents are closely related, a brief description of U. S. Pat. 2,684,870 will suffice to describe the closest prior art to Applicant's invention. This patent describes an improved selective adsorption process in which the granual adsorbent is conv~yed upwardly through a lift line and downwardly through an adsorption column in substantially the same condition of solids bulk density. It has been found that a conduit may be maintained with a vertically rising mass of solid granular adsorbent In which the bulk density of the solids is subs~antially the same as the bulk density of the solids when at rest as static bulk density.
This is accomplished by forcing a flow of lift gas upward1y through the interstices of the granules to establish frictional forces (indicated by the pressure differential) wh;ch ar~ sufficient to overcome the gravitational ~, .. .
~3~ 76R25/77Rl2 forces on the adsorbent granules as well as the frictional forces oF the con-duit walls on the moving bed of adsorbent and cause the mass to move upward.
The actual veloclty of the lift gas necessary ~o accompllsh this result is de pendent upon the s~ze and density of the granules, and the viscosity of the lift gas which is dlrectly determin~d by the pressure and temperature. The velocities are generally su~ficient tu cause fluidization of the adsorbent granules i~ thc adsorbent granules were ~nee to fluid~ze or becDme suspended in the lift gas.
All of the Berg patents relate primarily to Yerttcal movement Df solids in a continuous Flow loop. The Berg patents~ add1tionally, describe a vertical column that has a narrow opening at the bottom of the oolu~n and a wide spen~ng at ~he top, the column describing somewhat of a cone shape. -The reason for this is to prevent clogg~ng of the column as the granules are m~ved upwardly through the pipe. Thus, it can be seen that ln the Berg referencesl clogging of the column could occur.
The present disclosure relates to a dense-phase feeding of part~culate solids through horizontal and/or vertical feed pipes. Als~ the present in-vent~vn util~zes a ~a~l valve ~mmediately adjacent to the ~eeder ~x~t t~ all~w flow of sol-~d partlcles to be established. The Berg references heretofore described initiate f10w by simply prov~ding a pressure diffPrenti~l in the vertical ~eeder line. In the present ~nventlon, if a valve positioned at the exit of the feeder vessel is not used and flow is initiated by simply pressuri-zlng the feeder vessel, the feed llne will consistently plug. In add~tion, the Berg references employ a "thrust plate" or choke at the exit of the diverging vertical tube. The present ~nvent~on does not requ~re a choke to control ~low o~ dense-phase materlal through the feeder l~nes.
-3-~.C~ lZ 76R25/77R12 Sumnary of the Invention _.
A dense~phase particulate solids feeder and flow splitter apparatus, the combination consisting of a feeder vessel hav;ng a first sealable inlet end and a second outlet end, with a valve posi~oned adJacent ~o the outlet of the feeder vesse7, and an inlet end of a downstream feeder line. A pressure inlct line connected to ~h~ feeder vessel, the feeder vesse1 being pressurized throughsaid pressure inlet line, aft~r the vessel is filled wikh the particula~e solidswith the valve turned ~o a closed pos~tion and the vessel 1s subsequently sealed, to a pressure above the pressure in the feeder line downstream of the valve. A flow splitter housing having firs~ and second ends is connec~ed to a second end of the feeder line~ the housing forming a mani~old thereby. The second end of the housing having a multiplicity of downstream diverg~ny ouklet feeder l~nes extending therefr~m, e~ch of the feeder lines arP ln co~nunicat;l~nwith a series of separate diverglng channels formed in the seoond end oF the houslng ~hat inter~ect the center of the manifold in a oone, ~he apex of the cone facing the outlet o~ the feeder line connected to the housin~3 the apex serving to diver~ par~iculate solids passin~ through said flow splitter housing equally be~ween inlet ends of the separate dlverging channels toward the multi pticity of outlet feeder l~nes when the valve adjacent the feeder vessel is 2~ opened.
A coal feeder system is d~sclosed wherein a coal feeder bin is pressurized by introduc~ng gas to the top of the feeder vessel containing pulverized coal, the vessel be~ng adapted to flow the pulverized coal out of the bo~tom of ~he vessel. A ball valve or other full opening valve ~s posi~ioned at the bottom of the ccal feeder bin wh~oh allows the ~eeder vessel to be pressurized prior toinitia~ion of ~low. In srder to establish and maintain an adequate flow, ade-quate pressure drop must be created be~ween the f2eder bin and ~he feeder line .~
downstrea~. ~;thout the valve or an adequate prPssure drop between the feeder b;n and the feeder line, the feed line would frequently pluy. An even ~low of dense-phase c~al particles is essential when direc~ed into a coal splitter t~
assure an even distribution between a multiplicity of separa~e coal feed lines diverging from the coal splitter apparatus.
Pulverized coal with a mass-median size, for example, of 50 to 170 microns is placed in the coal feeding vessel. I~ has been determined that the coal with these average particle sizes will flow readily as long as the coal is suf-ficiently dispersed in a carrier gas to prevent intimate particle-to-par~icle contact. ~uccessful flow ~ests were made utilizing th;s sys~em to obtaln coal flow rates of 0.1 to about 10 lbs/sec with a pressure drop ~n the ~eeder tube of 5 to about 100 psl over line lengths from a few feet to about 80 feet. The gas flow rate necessary to transport the finely divided doal was found to be very small. This ~low rate was inferred from the vclum~trlc flow r~te into the column by subtractin~ the volume of the coal dispersed ~rom the column. The results indicate that on the average only the gas in the înterstices of the coala~ its co~pressed bulk density is carried with the coal.
The feed system has been successfully used with pulverized coal and several transport gases. Tests were run with a feeder coal particulate carrier gas of ni~rogen, helium, and carbon dioxide as well as hydrogen.
~here ~t is desirable to transport particulate materials such as coal particles from a feeder at max~mum solid density and with a minimum amount of gas for transport of the solid, the foregoing sys~em is i~eal. The feed system is currently being u~ilized to feed pulverized coal in~o a single ~njec~or elemen~ liquefact~on or gasification reac~or, and has been addit;onally success-fully demonstrated in com~inat~on with a coa1 splitter assembly whereby an even distributiQn of coal was fed to six indivldual injector elements. The feeder sys~em comprlses a vessel which ~s pressuri~ed, a gas source for pressurization~
and an outlet line with a relatively full opening ball valve located immediately adjacent to the feeder. A 11ne downstream of the valve feeds into, for example, a coal splitter assem~ly heretofore mentioned.
The feeder is operated by loading the vessel with particulate material such as pulverized coal and pres~urlzing ~o a level determined by the pressure drop in the outlet line and the downstream pressure, and opening the ~all valve to allow the mater;al to flow out towards the splitter assembly. The valve, clos~-coupled to the feeder3 and a relat;vely empty downstream line when flow is initiated are essential to the successful operation of the foreg~ing system. If the line between the feeder and the valve is too 10ng, the particulate material will pack in the l;ne and prevent flsw of ~he materialO However, if the full-opening valve is ct~se-coupled ~o the feeder vessel and the ; downstream line is initially free of solids~ the pulYerized coal material will ~low readily from the feeder at its bulk density towards the coal spli~ter apparatus. A consistent flow of dense-phase coal is essent;al ~or an even distributi~n of c~al particles ;n each of the separated coa~ distribution lines downstream of the spl;tter apparatus.
For example3 ;f the coal splitter divides the incoming coal particles from the single feed line frDm-the feeder vessel into six e~ual distr;bution feed lines, each of these feed lines terminate at an injectcr face~ Each o~ the six feed lines may have separate impinging ; streams uf hot hydr~gen downstream D~ the injector face; the hydrGgenation process taking place in a downstream reaction chamber.
2S The reac~ion o~ hot hydrogen and dense-phase coal particles is controlled to a specific residence time by quenching the react;ng products as they exit the reactiDn chamber.
Thercfore, it is an object of this inven~ion to provide a feed system to fluw particulate solid materials at essentially ~he;r bulk density with a small amount of carrier gas wi~hout plugging to a flow splitter ~o feed a multiplicityof injector elements by providlng a quick opening valve immed1ately downstream of a feeder bin and by providing a pressure differential between the feed bin and the feed line to the ~low splitter, Thus, it is an advan~age over the prior art to provide ~ dense-phase particulate solid feeder and coal splitter system that will not plu9 by pro-Yiding a quick openln~ valve immediately adjacent to the feed bin.
Yet another advantage over the prior art ls ~he abllity ~o flow solid particulate material in feed lines oriented in any d~rection, not just in a vertical direc~ion as taught by the prior ar~.
Although thls invention has been applied to pulverized coal, it will also operate successfully with a ~ariety of other pulverized or gr~nu1ar mater~als.
The abo~e-noted objects and advantages of the present in~ention will be more ful~y understood upon a study of the following detailed descrlptton ~n conjunction with the detailed drawings.
Brief Description of the Drawings FIG. l is a schematic diagram of the dense-phase part~culate solids feeder and flow splitter combination as it relates to a coal hydrngenation process9 FIG. 2 is a sect~on taken along l~nes 2-2 of FIG. l of the coal splitter apparatus, FIG. 3 is a section taken along lines 3-3 of FIG. 2 illustratin9 the coal splitter apparatus~ and FIG. 4 is a cross-seftlon of a typical coal hydrogenation inJector assembly that is attached to the separate coal feed lines from the splitter apparatus.
rrhe invention consists in the method of transporting particulate solids in dense-phase flow comprising the steps o:E:
filling a feeder vessel with particulate solids~
sealing said feeder vessel:
delivering carrier gas into said sealed feeder ves~
sel through a pressure inlet line in an amount to provide an initial pressure in excess of that in a downstream feeder line;
opening a valve connecting a lower portion of the feeder ve~sel to said downstream feeder line so as to dis-charge said solids at their bulk density by -the pressure differential and re~ultant expansion of the gas in the in~er-stices of said particulate solids; and delivering additonal c~rrier gas only into an upper portion of said vessel and in an amount both to maintain a pressure dif~erential between said vessel and said feeder line and to cause the solids to flow from said vessel through said valve and feeder line at their bul.k densi-ty, substantially the only carrier gas carried with the solids during discharge being that contained in the interstices.
-7~-76R2~/77R12 E~on of the Preferred Embodiments . .
Turning to the schematlc of FIG. 1, the dense-phase particulate solids feeder and flow splitter combination generally designated as 10 consists of a coa1 feed hopper 12, housing 14, sealable lid 16 at the uppermost portion of hopper 12, and a conical bottom section 18 to direct, for example, fine particles of coal towards the bottom of the feeder. A ball valve 26, for example, is placed immediately adjacent tQ the end oF the truncated cDnical section 18 of the housing 14. A gas pressurizing line 20 where, for example, ~N2, H2 or other gasses may be directed into the in~erior oF the coal feed hopper 12 after it is filled to provide a pressure di~ferential between the ~nterior of the coal Feed hopper 12 and the downstream l~ne 28 in communica~ion with valve 26. Valve 26 is normally closed during filling of the ~eed hopper 12. When the hopper is filled, lid 16 is then secured at the top of ~he hopper sPaling the feeder ves~el and the pressurizing gas is subsequen~ly fed into line 20 to the inter~or of the vessel. A series of gauges 221 23" 24 and 32 ~ may be used to mon~tor the pressures in the various parts of the dense-phase : particulate fe~der combination 10. A feed line 28 is connected between the downs~ream side of ball valve 26 and the t~p of the coal splltter apparatus generally des~gnated as 34. The splitter device evenly divides fine particl~te solids into each of feed lines 52 extending from the bottom of the coal split~er 34. Each of the diverging coal splitter tubes lead in~ an ~njector de~ice generally des~gnated as 54 to provide an equal amount of dense-phase coal to the base o~ the injectGr (FXG.4). A source of hot hydrogen is fed into line 56 ~o the interior of the injectDr 5q~and the hot hydrogen and ;njected coal particles are subsequently intermingl~d within the inter7nr of the re-action chamber generally designated as 58. The hydrDgenated products exit ~he reaction chamber at the base Df the chamber (n~t shown), and are quenched by quench source 60 to arrest the hydrogenation process at a predetermined short residence time period, and the resultant product is deposited within collection tank 62 downstream of quench means 60. Line 64 from the collection tank 62 -taps off the reacted products to, for example, cyclone separators, condensers, gas samplers, etc., none of ~hich are shown.
In operation, the coal feed hopper 12 is Eilled with finely divided coal particles such as, for example, 70% minus 200 mesh. After the hopper is filled (ball valve 26 being in the closed position), the top o the hopper 16 is sealed and a gas such as GN~ is admitted through line 20 tO the interiox of the coal hopper to a predetermined pressure. Tests have been performed with a hopper pressure as low as 7 psi, but typically 20 to 100 psi, and a downstream pressure of ambient in line 28 below valve 26. The differential between the in~erior of the hopper 12 and the interior of the line 28 emanating ~rom the downstream end of valve 26 provides the dri~ing force for the particulate coal particles when ball valve 26 is open. After the pressure differential is established by monitoring gauge 23, valve 26 is opened to adm.it coal to the downstream line 28. The coal flows rapidly (for example,2~0 lb/hr through a 3/8 inch line) towards the coal splitter 34~ the splitter 34 then divides the constan-t ~lowing coal particles evenly be-tween the respectiwe channels 40 in the coal splitter housing 36 (FIGS. 2 and 3) towards the injector 54 via feed tubes 52 emanating from the base 41 of thP splitter body 36.
: At the same time, hot hydrogen is admitted to ~he interior of the injector 54 through line 56, the hot hydrogen then passes through orifice 84 to impinge with the coal particles injected below the injector face 80 (FIG. 4) ~o react wi-thin the interior of reaction chamber 58~ The reacting products are subsequently quenched by quench source 60 and are collected within collection bin 62.
It is to be noted tha-t the flow density of the solids and gas discharged from the ~eed hopper or feeder vessel 12 is up to about 1000 lbs. solids per lb. gas.
_ 9 7~R25/77R12 Upon shutdown of ball valve 26, a purge line 30 ls activated wherein, for example, GN2 ~5 admitted below valve 26 to clear line 28 -Prom any residual coal particles tha~ might be remaining. The ~ner~ gas simply cleans ~he passages in line 28, coal splitter 34, ~njec~or 54, and ~n~o ~he interior of the react~on chamber 58 in preparation for subsequent operation of the hydro genation process. An on~o~f valve 31 is provided within line 30 to readily accommodate this line purge process.
Turning now to FIGS. 2 and 3~ a deta~l drawing af ~he coal ~plltter apparatus is shown wherein the coal splitter generally designated as 34 con-sists of a hous~ng 36 and which is conneoted or otherwtse metallurg~cally bonded to the end of coal feed line 28. Within the end of the coal feed line 28 is defined a chamber or man~fold 38. Coal splitter body 36 1s formed ~n a general conical shape. Each of the mul~plic~ty ~f channels 40 are dr~lled through the body 36 from the base side 41 in such a manner that each ~f the channels intersect the centerllne of the attached feed line 28. Machined int~
the top of the body 36 are a multiplie~ty of conical shaped coun~ersink~ (B) wh~ch intersect the centerline of ind~vidual channels 40 at points ~A). The equally spaced countersinks (B) machined into the top of body 36 for~ a natural trough or channel defined by ridge lines 44 and surface 46 to provide a means to direct the coal partlcles evenly between each of the channels 40 in conical block 36~ When view~ng FIG. 3 it can readily be seen ~hat surface 46 ls formed by conical countersinks (B~ maohined into the top of ~he con~cal block 36.
Ridge llnes 44 formed by the ;ntersection of adjacent countersinks ~B) thus pro-vide natural separating rldges to distribute the consistently ~lowing dense-phase cval part~cles evenly between all of the channels 4D in block 363 thus the c~al splitter 34 provld~s an even amount of coal at a constant r~te towards the down-s~ream mul~lple passage injector. The apex 42 ls na~urally formed by the 76R25/77Rl2 slmultaneous întersec~ion of the equidistantly-spaced countersinks (B) at ~he centerline oF block 36. ~hen the last coun~ersink ~s machlned the apex 42 is formed, thus ~he coal, as lt enters ~he coal spl~ter, strikes ~he apex and ~s div~ded equally be~ween the individual channe1s 40. It can be seen that the entire top surface of block 36 ts formed by the machining of counters~nks ~B~, leav~ng no blunt edges tha~ migh~ cause coal clogg~ng.
Turn~ng now to FIG. 4, each of the coal feed lines 52 emanating from base 41 of body 36 lead towards an Injec~or housing generally designated as ~4.
Lines 52 at their uppermos~ ends are metal1urgically ~onded within socket 48 ~n the base 41 of block 36. The feed lines 52 are ~hen bonded to short coal feed studs 76 in injector hous~ng 54 that traverse through upper surface 72 of in-jector body 70 int~ ~he ~njector face 80. A chamber 74 ~s fDrmed by thc inj~ctor body 70. Hot hydrogen feed line 56 oommunlcates w~th chamber 74 to prov~de a source of hot hydrogen for the sol~d par~cu7ate coal. A seri~s of or~fices 84 are ~rovided through the ~nJector face 8D at an implngement ~ngle so that each coal feed tube 76 ls provlded a source of hot hydr~gen. These hole patterns for hot hydrogen may be twc~on-one9 or three on-one, or four~on-one dependent upon the mlxture ratio deslred with~n the reaction chamber generally designated as 58. A two-on-one pattern is shown, ~or example, ln the cross-sectlon of ~IG. 4.
An examp~e of the value of diYld~ng sDllds flow t~ multiple injectio~ pro-cess has ~een demonstrated in a coal combust1On exper~ment. In th~s appl~cation a six-element ~nject~on pattern was required to prov~de a very uniform m~xing dlstributlon ln a combllstion chamber. A six-element spli~er was used ~o pro-2S vide equal flowrate to each o~ the injectlon elemen~s and the gaseous reactant in this case was pressurized ailr. Another related appllcat50n planned for this Feeding and d~v5ding ~echn~que ~s for ~njectlon of "seed" ma~erials (pota~sium or ceasium c~mpounds ln powder form) in~o combust~on chambers fsr mayne~o hydro dynamic general;ors. Aga1n, ~he reason ~s tc proYide uni~orm dis~ribu~on of ~he mater~als by ~n~ect~ng equal amsunts at numerous locat;ons, During operation, as the coal is directed thrvugh coal pipes 52 into the short studs 76 within body 70, ~he hot hydrogen is generally simul~aneously initiated3 ~hus directing hot hydrogen through orifices 84 into the reaction manifold 90 defined by the react~on chamber walls 58. The angle 86 determines the point of impingement 88 of the hot hydrogen wi~h the exiking coal particles from the end 77 of ~he coal feed t~be 76. Impingemen~, for example, may occur approximately one-half inch below the face of the injector.
Obviously, other types of injeotors may be shown. For example, each o~
the coa1 feed studs 76 could be surrounded by concentric opening in the in-jector face 80 whereby the hot hydrogen simply passes by the outer walls of the studs 76 and intermingles with the coal partic~es downstream ~f the 1njector face 80 as taught by cc-pending application, 5erial Number 689,002.
It is additionally obvious that other configurations of injectors may be utilized whereby it is neoessary to provide a mul~7plicity of dense-phase s~urces ~ coal toward an injector.
It will, of course, be realized that various modifications can be made in the design and operation of the present invention without departing from the spirit thereof. Thus~ while the principal, preferred c~nstruetion, and mode ~ operatian of the invention have been expla~ned and what is now considere~ to represent its best embodiment has been illustrated and described, it should be understood that within t~e sc~pe of the appended claims the invent~on may be practiced otherwisP than as specifica11y illustrated and descr;bed.
A dense~phase particulate solids feeder and flow splitter apparatus, the combination consisting of a feeder vessel hav;ng a first sealable inlet end and a second outlet end, with a valve posi~oned adJacent ~o the outlet of the feeder vesse7, and an inlet end of a downstream feeder line. A pressure inlct line connected to ~h~ feeder vessel, the feeder vesse1 being pressurized throughsaid pressure inlet line, aft~r the vessel is filled wikh the particula~e solidswith the valve turned ~o a closed pos~tion and the vessel 1s subsequently sealed, to a pressure above the pressure in the feeder line downstream of the valve. A flow splitter housing having firs~ and second ends is connec~ed to a second end of the feeder line~ the housing forming a mani~old thereby. The second end of the housing having a multiplicity of downstream diverg~ny ouklet feeder l~nes extending therefr~m, e~ch of the feeder lines arP ln co~nunicat;l~nwith a series of separate diverglng channels formed in the seoond end oF the houslng ~hat inter~ect the center of the manifold in a oone, ~he apex of the cone facing the outlet o~ the feeder line connected to the housin~3 the apex serving to diver~ par~iculate solids passin~ through said flow splitter housing equally be~ween inlet ends of the separate dlverging channels toward the multi pticity of outlet feeder l~nes when the valve adjacent the feeder vessel is 2~ opened.
A coal feeder system is d~sclosed wherein a coal feeder bin is pressurized by introduc~ng gas to the top of the feeder vessel containing pulverized coal, the vessel be~ng adapted to flow the pulverized coal out of the bo~tom of ~he vessel. A ball valve or other full opening valve ~s posi~ioned at the bottom of the ccal feeder bin wh~oh allows the ~eeder vessel to be pressurized prior toinitia~ion of ~low. In srder to establish and maintain an adequate flow, ade-quate pressure drop must be created be~ween the f2eder bin and ~he feeder line .~
downstrea~. ~;thout the valve or an adequate prPssure drop between the feeder b;n and the feeder line, the feed line would frequently pluy. An even ~low of dense-phase c~al particles is essential when direc~ed into a coal splitter t~
assure an even distribution between a multiplicity of separa~e coal feed lines diverging from the coal splitter apparatus.
Pulverized coal with a mass-median size, for example, of 50 to 170 microns is placed in the coal feeding vessel. I~ has been determined that the coal with these average particle sizes will flow readily as long as the coal is suf-ficiently dispersed in a carrier gas to prevent intimate particle-to-par~icle contact. ~uccessful flow ~ests were made utilizing th;s sys~em to obtaln coal flow rates of 0.1 to about 10 lbs/sec with a pressure drop ~n the ~eeder tube of 5 to about 100 psl over line lengths from a few feet to about 80 feet. The gas flow rate necessary to transport the finely divided doal was found to be very small. This ~low rate was inferred from the vclum~trlc flow r~te into the column by subtractin~ the volume of the coal dispersed ~rom the column. The results indicate that on the average only the gas in the înterstices of the coala~ its co~pressed bulk density is carried with the coal.
The feed system has been successfully used with pulverized coal and several transport gases. Tests were run with a feeder coal particulate carrier gas of ni~rogen, helium, and carbon dioxide as well as hydrogen.
~here ~t is desirable to transport particulate materials such as coal particles from a feeder at max~mum solid density and with a minimum amount of gas for transport of the solid, the foregoing sys~em is i~eal. The feed system is currently being u~ilized to feed pulverized coal in~o a single ~njec~or elemen~ liquefact~on or gasification reac~or, and has been addit;onally success-fully demonstrated in com~inat~on with a coa1 splitter assembly whereby an even distributiQn of coal was fed to six indivldual injector elements. The feeder sys~em comprlses a vessel which ~s pressuri~ed, a gas source for pressurization~
and an outlet line with a relatively full opening ball valve located immediately adjacent to the feeder. A 11ne downstream of the valve feeds into, for example, a coal splitter assem~ly heretofore mentioned.
The feeder is operated by loading the vessel with particulate material such as pulverized coal and pres~urlzing ~o a level determined by the pressure drop in the outlet line and the downstream pressure, and opening the ~all valve to allow the mater;al to flow out towards the splitter assembly. The valve, clos~-coupled to the feeder3 and a relat;vely empty downstream line when flow is initiated are essential to the successful operation of the foreg~ing system. If the line between the feeder and the valve is too 10ng, the particulate material will pack in the l;ne and prevent flsw of ~he materialO However, if the full-opening valve is ct~se-coupled ~o the feeder vessel and the ; downstream line is initially free of solids~ the pulYerized coal material will ~low readily from the feeder at its bulk density towards the coal spli~ter apparatus. A consistent flow of dense-phase coal is essent;al ~or an even distributi~n of c~al particles ;n each of the separated coa~ distribution lines downstream of the spl;tter apparatus.
For example3 ;f the coal splitter divides the incoming coal particles from the single feed line frDm-the feeder vessel into six e~ual distr;bution feed lines, each of these feed lines terminate at an injectcr face~ Each o~ the six feed lines may have separate impinging ; streams uf hot hydr~gen downstream D~ the injector face; the hydrGgenation process taking place in a downstream reaction chamber.
2S The reac~ion o~ hot hydrogen and dense-phase coal particles is controlled to a specific residence time by quenching the react;ng products as they exit the reactiDn chamber.
Thercfore, it is an object of this inven~ion to provide a feed system to fluw particulate solid materials at essentially ~he;r bulk density with a small amount of carrier gas wi~hout plugging to a flow splitter ~o feed a multiplicityof injector elements by providlng a quick opening valve immed1ately downstream of a feeder bin and by providing a pressure differential between the feed bin and the feed line to the ~low splitter, Thus, it is an advan~age over the prior art to provide ~ dense-phase particulate solid feeder and coal splitter system that will not plu9 by pro-Yiding a quick openln~ valve immediately adjacent to the feed bin.
Yet another advantage over the prior art ls ~he abllity ~o flow solid particulate material in feed lines oriented in any d~rection, not just in a vertical direc~ion as taught by the prior ar~.
Although thls invention has been applied to pulverized coal, it will also operate successfully with a ~ariety of other pulverized or gr~nu1ar mater~als.
The abo~e-noted objects and advantages of the present in~ention will be more ful~y understood upon a study of the following detailed descrlptton ~n conjunction with the detailed drawings.
Brief Description of the Drawings FIG. l is a schematic diagram of the dense-phase part~culate solids feeder and flow splitter combination as it relates to a coal hydrngenation process9 FIG. 2 is a sect~on taken along l~nes 2-2 of FIG. l of the coal splitter apparatus, FIG. 3 is a section taken along lines 3-3 of FIG. 2 illustratin9 the coal splitter apparatus~ and FIG. 4 is a cross-seftlon of a typical coal hydrogenation inJector assembly that is attached to the separate coal feed lines from the splitter apparatus.
rrhe invention consists in the method of transporting particulate solids in dense-phase flow comprising the steps o:E:
filling a feeder vessel with particulate solids~
sealing said feeder vessel:
delivering carrier gas into said sealed feeder ves~
sel through a pressure inlet line in an amount to provide an initial pressure in excess of that in a downstream feeder line;
opening a valve connecting a lower portion of the feeder ve~sel to said downstream feeder line so as to dis-charge said solids at their bulk density by -the pressure differential and re~ultant expansion of the gas in the in~er-stices of said particulate solids; and delivering additonal c~rrier gas only into an upper portion of said vessel and in an amount both to maintain a pressure dif~erential between said vessel and said feeder line and to cause the solids to flow from said vessel through said valve and feeder line at their bul.k densi-ty, substantially the only carrier gas carried with the solids during discharge being that contained in the interstices.
-7~-76R2~/77R12 E~on of the Preferred Embodiments . .
Turning to the schematlc of FIG. 1, the dense-phase particulate solids feeder and flow splitter combination generally designated as 10 consists of a coa1 feed hopper 12, housing 14, sealable lid 16 at the uppermost portion of hopper 12, and a conical bottom section 18 to direct, for example, fine particles of coal towards the bottom of the feeder. A ball valve 26, for example, is placed immediately adjacent tQ the end oF the truncated cDnical section 18 of the housing 14. A gas pressurizing line 20 where, for example, ~N2, H2 or other gasses may be directed into the in~erior oF the coal feed hopper 12 after it is filled to provide a pressure di~ferential between the ~nterior of the coal Feed hopper 12 and the downstream l~ne 28 in communica~ion with valve 26. Valve 26 is normally closed during filling of the ~eed hopper 12. When the hopper is filled, lid 16 is then secured at the top of ~he hopper sPaling the feeder ves~el and the pressurizing gas is subsequen~ly fed into line 20 to the inter~or of the vessel. A series of gauges 221 23" 24 and 32 ~ may be used to mon~tor the pressures in the various parts of the dense-phase : particulate fe~der combination 10. A feed line 28 is connected between the downs~ream side of ball valve 26 and the t~p of the coal splltter apparatus generally des~gnated as 34. The splitter device evenly divides fine particl~te solids into each of feed lines 52 extending from the bottom of the coal split~er 34. Each of the diverging coal splitter tubes lead in~ an ~njector de~ice generally des~gnated as 54 to provide an equal amount of dense-phase coal to the base o~ the injectGr (FXG.4). A source of hot hydrogen is fed into line 56 ~o the interior of the injectDr 5q~and the hot hydrogen and ;njected coal particles are subsequently intermingl~d within the inter7nr of the re-action chamber generally designated as 58. The hydrDgenated products exit ~he reaction chamber at the base Df the chamber (n~t shown), and are quenched by quench source 60 to arrest the hydrogenation process at a predetermined short residence time period, and the resultant product is deposited within collection tank 62 downstream of quench means 60. Line 64 from the collection tank 62 -taps off the reacted products to, for example, cyclone separators, condensers, gas samplers, etc., none of ~hich are shown.
In operation, the coal feed hopper 12 is Eilled with finely divided coal particles such as, for example, 70% minus 200 mesh. After the hopper is filled (ball valve 26 being in the closed position), the top o the hopper 16 is sealed and a gas such as GN~ is admitted through line 20 tO the interiox of the coal hopper to a predetermined pressure. Tests have been performed with a hopper pressure as low as 7 psi, but typically 20 to 100 psi, and a downstream pressure of ambient in line 28 below valve 26. The differential between the in~erior of the hopper 12 and the interior of the line 28 emanating ~rom the downstream end of valve 26 provides the dri~ing force for the particulate coal particles when ball valve 26 is open. After the pressure differential is established by monitoring gauge 23, valve 26 is opened to adm.it coal to the downstream line 28. The coal flows rapidly (for example,2~0 lb/hr through a 3/8 inch line) towards the coal splitter 34~ the splitter 34 then divides the constan-t ~lowing coal particles evenly be-tween the respectiwe channels 40 in the coal splitter housing 36 (FIGS. 2 and 3) towards the injector 54 via feed tubes 52 emanating from the base 41 of thP splitter body 36.
: At the same time, hot hydrogen is admitted to ~he interior of the injector 54 through line 56, the hot hydrogen then passes through orifice 84 to impinge with the coal particles injected below the injector face 80 (FIG. 4) ~o react wi-thin the interior of reaction chamber 58~ The reacting products are subsequently quenched by quench source 60 and are collected within collection bin 62.
It is to be noted tha-t the flow density of the solids and gas discharged from the ~eed hopper or feeder vessel 12 is up to about 1000 lbs. solids per lb. gas.
_ 9 7~R25/77R12 Upon shutdown of ball valve 26, a purge line 30 ls activated wherein, for example, GN2 ~5 admitted below valve 26 to clear line 28 -Prom any residual coal particles tha~ might be remaining. The ~ner~ gas simply cleans ~he passages in line 28, coal splitter 34, ~njec~or 54, and ~n~o ~he interior of the react~on chamber 58 in preparation for subsequent operation of the hydro genation process. An on~o~f valve 31 is provided within line 30 to readily accommodate this line purge process.
Turning now to FIGS. 2 and 3~ a deta~l drawing af ~he coal ~plltter apparatus is shown wherein the coal splitter generally designated as 34 con-sists of a hous~ng 36 and which is conneoted or otherwtse metallurg~cally bonded to the end of coal feed line 28. Within the end of the coal feed line 28 is defined a chamber or man~fold 38. Coal splitter body 36 1s formed ~n a general conical shape. Each of the mul~plic~ty ~f channels 40 are dr~lled through the body 36 from the base side 41 in such a manner that each ~f the channels intersect the centerllne of the attached feed line 28. Machined int~
the top of the body 36 are a multiplie~ty of conical shaped coun~ersink~ (B) wh~ch intersect the centerline of ind~vidual channels 40 at points ~A). The equally spaced countersinks (B) machined into the top of body 36 for~ a natural trough or channel defined by ridge lines 44 and surface 46 to provide a means to direct the coal partlcles evenly between each of the channels 40 in conical block 36~ When view~ng FIG. 3 it can readily be seen ~hat surface 46 ls formed by conical countersinks (B~ maohined into the top of ~he con~cal block 36.
Ridge llnes 44 formed by the ;ntersection of adjacent countersinks ~B) thus pro-vide natural separating rldges to distribute the consistently ~lowing dense-phase cval part~cles evenly between all of the channels 4D in block 363 thus the c~al splitter 34 provld~s an even amount of coal at a constant r~te towards the down-s~ream mul~lple passage injector. The apex 42 ls na~urally formed by the 76R25/77Rl2 slmultaneous întersec~ion of the equidistantly-spaced countersinks (B) at ~he centerline oF block 36. ~hen the last coun~ersink ~s machlned the apex 42 is formed, thus ~he coal, as lt enters ~he coal spl~ter, strikes ~he apex and ~s div~ded equally be~ween the individual channe1s 40. It can be seen that the entire top surface of block 36 ts formed by the machining of counters~nks ~B~, leav~ng no blunt edges tha~ migh~ cause coal clogg~ng.
Turn~ng now to FIG. 4, each of the coal feed lines 52 emanating from base 41 of body 36 lead towards an Injec~or housing generally designated as ~4.
Lines 52 at their uppermos~ ends are metal1urgically ~onded within socket 48 ~n the base 41 of block 36. The feed lines 52 are ~hen bonded to short coal feed studs 76 in injector hous~ng 54 that traverse through upper surface 72 of in-jector body 70 int~ ~he ~njector face 80. A chamber 74 ~s fDrmed by thc inj~ctor body 70. Hot hydrogen feed line 56 oommunlcates w~th chamber 74 to prov~de a source of hot hydrogen for the sol~d par~cu7ate coal. A seri~s of or~fices 84 are ~rovided through the ~nJector face 8D at an implngement ~ngle so that each coal feed tube 76 ls provlded a source of hot hydr~gen. These hole patterns for hot hydrogen may be twc~on-one9 or three on-one, or four~on-one dependent upon the mlxture ratio deslred with~n the reaction chamber generally designated as 58. A two-on-one pattern is shown, ~or example, ln the cross-sectlon of ~IG. 4.
An examp~e of the value of diYld~ng sDllds flow t~ multiple injectio~ pro-cess has ~een demonstrated in a coal combust1On exper~ment. In th~s appl~cation a six-element ~nject~on pattern was required to prov~de a very uniform m~xing dlstributlon ln a combllstion chamber. A six-element spli~er was used ~o pro-2S vide equal flowrate to each o~ the injectlon elemen~s and the gaseous reactant in this case was pressurized ailr. Another related appllcat50n planned for this Feeding and d~v5ding ~echn~que ~s for ~njectlon of "seed" ma~erials (pota~sium or ceasium c~mpounds ln powder form) in~o combust~on chambers fsr mayne~o hydro dynamic general;ors. Aga1n, ~he reason ~s tc proYide uni~orm dis~ribu~on of ~he mater~als by ~n~ect~ng equal amsunts at numerous locat;ons, During operation, as the coal is directed thrvugh coal pipes 52 into the short studs 76 within body 70, ~he hot hydrogen is generally simul~aneously initiated3 ~hus directing hot hydrogen through orifices 84 into the reaction manifold 90 defined by the react~on chamber walls 58. The angle 86 determines the point of impingement 88 of the hot hydrogen wi~h the exiking coal particles from the end 77 of ~he coal feed t~be 76. Impingemen~, for example, may occur approximately one-half inch below the face of the injector.
Obviously, other types of injeotors may be shown. For example, each o~
the coa1 feed studs 76 could be surrounded by concentric opening in the in-jector face 80 whereby the hot hydrogen simply passes by the outer walls of the studs 76 and intermingles with the coal partic~es downstream ~f the 1njector face 80 as taught by cc-pending application, 5erial Number 689,002.
It is additionally obvious that other configurations of injectors may be utilized whereby it is neoessary to provide a mul~7plicity of dense-phase s~urces ~ coal toward an injector.
It will, of course, be realized that various modifications can be made in the design and operation of the present invention without departing from the spirit thereof. Thus~ while the principal, preferred c~nstruetion, and mode ~ operatian of the invention have been expla~ned and what is now considere~ to represent its best embodiment has been illustrated and described, it should be understood that within t~e sc~pe of the appended claims the invent~on may be practiced otherwisP than as specifica11y illustrated and descr;bed.
Claims (5)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. The method of transporting particulate solids in dense-phase flow comprising the steps of:
filling a feeder vessel with particulate solids;
sealing said feeder vessel;
delivering carrier gas into said sealed feeder vessel through a pressure inlet line in an amount to provide an initial pressure in excess of that in a downstream feeder line;
opening a valve connecting a lower portion of the feeder vessel to said downstream feeder line so as to discharge said solids at their bulk density by the pressure differential and resultant expansion of the gas in the interstices of said particulate solids; and delivering additional carrier gas only into an upper portion of said vessel and in an amount both to maintain a pressure differential between said vessel and said feeder line and to cause the solids to flow from said vessel through said valve and feeder line at their bulk density, substantially the only carrier gas carried with the solids during discharge being that contained in the interstices.
filling a feeder vessel with particulate solids;
sealing said feeder vessel;
delivering carrier gas into said sealed feeder vessel through a pressure inlet line in an amount to provide an initial pressure in excess of that in a downstream feeder line;
opening a valve connecting a lower portion of the feeder vessel to said downstream feeder line so as to discharge said solids at their bulk density by the pressure differential and resultant expansion of the gas in the interstices of said particulate solids; and delivering additional carrier gas only into an upper portion of said vessel and in an amount both to maintain a pressure differential between said vessel and said feeder line and to cause the solids to flow from said vessel through said valve and feeder line at their bulk density, substantially the only carrier gas carried with the solids during discharge being that contained in the interstices.
2. The method of Claim l wherein said particulate solids have a mass-median size of from about 50 to 170 microns.
3. The method of Claim l wherein the pressure differential between said feeder vessel and said downstream feeder line is maintained in the range of from about 7 to about 100 psig.
4. The method of Claim 1 wherein the flow density of said solids and gas discharges from said vessel is up to about 1000 lbs.
solids per lb. gas.
solids per lb. gas.
5, The method of Claim 3 wherein the flow density of said solids and gas discharged from said vessel is up to about 1000 lbs.
solids per lb. gas.
solids per lb. gas.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US81930777A | 1977-07-27 | 1977-07-27 | |
| US819,307 | 1977-07-27 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1094612A true CA1094612A (en) | 1981-01-27 |
Family
ID=25227780
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA298,592A Expired CA1094612A (en) | 1977-07-27 | 1978-03-09 | Dense-phase feeder method |
Country Status (7)
| Country | Link |
|---|---|
| JP (1) | JPS5427186A (en) |
| AU (1) | AU517772B2 (en) |
| CA (1) | CA1094612A (en) |
| DE (1) | DE2832846A1 (en) |
| FR (1) | FR2398681B1 (en) |
| GB (1) | GB1588553A (en) |
| IT (1) | IT1102474B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103466332A (en) * | 2013-08-26 | 2013-12-25 | 张家港保税区万盛机械工业有限公司 | Dense-phase compressed gas delivery device |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58164692A (en) * | 1982-03-25 | 1983-09-29 | Babcock Hitachi Kk | Supplying coal under stabilized condition by means of lock hopper |
| JPS5926437U (en) * | 1982-08-09 | 1984-02-18 | 住友金属工業株式会社 | Distributor |
| JPH0485438U (en) * | 1990-11-30 | 1992-07-24 | ||
| US8403602B2 (en) * | 2011-03-16 | 2013-03-26 | Babcock Power Services, Inc. | Coal flow splitters and distributor devices |
| CN115301175A (en) * | 2022-08-16 | 2022-11-08 | 华昌智典新材料(江苏)有限公司 | Production reation kettle for film forming auxiliary agent |
Family Cites Families (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE261540C (en) * | ||||
| DE498123C (en) * | 1926-06-15 | 1930-05-17 | Aeg | Firing system for powdery fuels, especially for coal dust |
| US1871853A (en) * | 1927-08-09 | 1932-08-16 | Joseph E Kennedy | Pneumatic transporting and distributing of pulverized material |
| GB293271A (en) * | 1928-01-10 | 1928-07-05 | Pulverised Coal Australasia Lt | Improved means for transporting pulverised coal and other powdered materials |
| DE648057C (en) * | 1932-05-27 | 1937-07-20 | Joseph Elliott Kennedy | Feeding and transport system for dust or the like influenced by compressed air. |
| DE629935C (en) * | 1935-04-21 | 1936-05-15 | Polysius Akt Ges G | Method for conveying bulk goods of all kinds using one or more pressure vessels |
| US2684870A (en) * | 1948-12-24 | 1954-07-27 | Union Oil Co | Conveyance of granular solids |
| US2684868A (en) * | 1951-01-16 | 1954-07-27 | Union Oil Co | Conveyance of granular solids |
| DE1767453A1 (en) * | 1968-05-11 | 1971-09-16 | Petrocarb Inc | Method and device for the pneumatic injection of solid particles into a high pressure zone |
| GB1151246A (en) * | 1966-11-14 | 1969-05-07 | William John Courtney Trythall | Improvements in or relating to Pneumatic Material Handling Systems |
| DE1556686C3 (en) * | 1968-02-21 | 1982-10-07 | Schaubstahl-Werke, 5910 Kreuztal | Transportable silo container with at least one outlet nozzle and pressure chamber (s) |
| US3554607A (en) * | 1968-10-23 | 1971-01-12 | Jetair Inc | Particulate material distributing apparatus |
| US4018671A (en) * | 1975-01-14 | 1977-04-19 | Marathon Oil Company | Intermittent catalyst addition system |
-
1978
- 1978-03-09 CA CA298,592A patent/CA1094612A/en not_active Expired
- 1978-03-10 AU AU34052/78A patent/AU517772B2/en not_active Expired
- 1978-03-17 GB GB10734/78A patent/GB1588553A/en not_active Expired
- 1978-03-28 JP JP3496378A patent/JPS5427186A/en active Granted
- 1978-03-31 FR FR7809632A patent/FR2398681B1/en not_active Expired
- 1978-04-04 IT IT48742/78A patent/IT1102474B/en active
- 1978-07-26 DE DE19782832846 patent/DE2832846A1/en not_active Ceased
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103466332A (en) * | 2013-08-26 | 2013-12-25 | 张家港保税区万盛机械工业有限公司 | Dense-phase compressed gas delivery device |
Also Published As
| Publication number | Publication date |
|---|---|
| DE2832846A1 (en) | 1979-02-15 |
| IT7848742A0 (en) | 1978-04-04 |
| IT1102474B (en) | 1985-10-07 |
| AU3405278A (en) | 1979-09-13 |
| JPS5427186A (en) | 1979-03-01 |
| FR2398681A1 (en) | 1979-02-23 |
| JPS636449B2 (en) | 1988-02-09 |
| AU517772B2 (en) | 1981-08-27 |
| GB1588553A (en) | 1981-04-23 |
| FR2398681B1 (en) | 1986-01-24 |
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