US2609282A - Apparatus and method for handling of liquefied normally gaseous materials - Google Patents

Description

Sept. 2, 1 J. s. HAUG ETAL APPARATUS AND METHOD FOR HANDLING OF LIQUEFIED NORMALLY GASEOUS MATERIALS 2 SHEETS--SHEE'I 1 Filed Dec. 51, 1946 R O T NG m WH S N H O v PRICE WJANEMWJR BY THEIR ATTORNEYS W6- Sept. 2, 1952 -J. s. HAUG ET AL 2,609,282

APPARATUS AND METHOD FOR HANDLING OF LIQUEFIED NORMALLY GASEOUS MATERIALS Filed Dec. 31, 1946 2 SHEETSSHEE'I 2 Ill TTT w 75 M72, 40:521. INVENTOR 0 /07 JOHN S,HAUG

PRICE WJANEWAYJR.

BY THEIR ATTORNEYS /5@ZOW7V&

l ate'n ted Sept. 2

OF LIQUEFIED NORMALLY GAS-EOUS MA- TERIALS John S. Haug, Philadelphia, and Price W. J aneway, Jr., Media, Pa., assignors to United Engineers & Constructors Inc., Philadelphia, Pa., a corporation of Delaware Application December 31, 1946, Serial No. 719,348

4 Claims. IV The present invention relates to the handling of liquids having a relatively high vapor pressure under the conditions obtaining.

An example of such handling is the'transportation through pipes exposed to atmospheric 5 pane vapor, small dififerences in percentage of conditions of liquid phase material normally evaporation by weight resulting in great difier'f gaseous under such conditions. ences in the proportion of vapor present by vol- For purposes of illustration, the invention will ume. Such a mixture cannot be accurately" be particularly described in connection with its metered by presently available liquid or vapor application to the piping and utilization of liquemeters, with the result that the rate of utilizafied normally gaseous hydrocarbons such as protion of the material may not be accurately known pane and butane, which are frequently employed or ascertained. as raw materials in the manufacture of com- One of the objects of the present invention is bustible gas. to provide a method of and apparatus for the One of the uses of such liquefied normally delivery through pipes of liquid material of relgaseous hydrocarbon material in the manufacatively high volatility under the ambient conture of combustible gas, is in the supplementing, ditions, in the use of which the liquid material 1 during periods of peak loads, of the carburetted delivered to a zone of utilization, treatment, or water gas normally produced in carburetted other disposal may be accurately metered in spite water gas sets from solid fuel and heavier hyof the formation of vapor phase occurring as a drocarbon oils. necessary incident to a drop in pressure in the Such utilization of liquefied normally gaseous transportation system. Other objects of the inhydrocarbons frequently includes the cracking of vention will appear as the specification proceeds. these materials by passage through the fuel bed For co e c e i v ntion Will be more. of the water gas generator in a step commonly particularly described in connection with the termed reforming, and may also include a step p p 0f liquefied P p rom Storage under of utilizing these materials for enrichment withpressure to utilization in the manufacture of car-' out material cracking. buretted water gas, and in connection with the It is economical from the standpoint of the description of the figures, which form a part of investment costs to store hydrocarbon materials this specifi and in which such as propane .and butane as liquids under Figure 1 WS. Somewhat at c l y. relatively elevated pressure because of the greatp y in elevation and p y in Vertical Seetion,v 1y reduced size of the storage equipment rea carburetted water gas set suppliedwith and quird to store these materials in gaseous form. utilizing liquefied propane in accordance with a.- It is also economical from the standpoint Of 111- form of the present invention chosen for illusvestment to transport these materials in liquid t t form, from storage to a point adjacent the g Figure 2 shows, somewhat diagrammatically, ggggg g i lgfi? gifii gg gg g p gg fgg fig partly in elevation and partly in vertical section, as compared with that required to transport 40 gfig i of the apparatus of the mventmn'. them as gases. r 3 h h Such liquid storage is customarily exposed to lgur'e T 0W5 aflpor {on of t e apparatus I existing atmospheric temperature conditions and Flgure Wlth P F QS' therefore the storage of the liquid usually oc- Referrmg Ftlgure 1: curs under a very considerable pressure due to generally mdlca'tes the generator 2 the car? 7 this temperature. For example, in the case of bummer 3 the Superheater a 4 the Wash commercial liquid propane, at say 30 F. the 0f ealburetted Water gas Setvapor pressure will be of the order of 100 pounds The generator is pr vid d wit an i nited fuel per square inch absolute, while at 72 F. the bed 5, ofsolid fuel,-such as coke, resting on a; vapor pressure will be of the order of 160 pounds gr t (not O D- The ator is furt er I per square inch absolute. Since the liquid in provided with air supply means and steamsup l storage is in equilibrium under the existing storply means 6 and 1 respectively, for upwardly air" age pressure and the existing atmospheric temblasting Stea g the fuel bed. The gen perature, any pressure difierential causing a fiow erator is also illustrated as provided with sec.- of the liquid from storage will cause the evapo- 2 r ration of a portion thereof. As a result, the material passing through the pipe leading from the storage vessel toward the point of utilization is a varying mixture of liquefied propane and proondary air supply means 8 and oil supply means 3 9 arranged to spray oil onto the top of the fuel bed.

The generator is further illustrated as provided with a gas take-off connection 10, leading from its upper portiorrto the upper portion of the carburetterZ, and with the gas take-off H, provided with valve Ila, and leading from its lower portion below the grate to the wash box 4.

The carburetter is illustrated as devoid of checker-brick, but provided with the refractory lining l2. [3 indicates an oil supply means arranged to spray oil into the carburetter. The base of the carguretter is illustrated as connected with the base of the superheater by the connection The superheater is illustrated as provided with refractory checker-brick l5, stack valve l6, and gas take-01f IT, provided with valve Ila, and leading from the upper portion of the superheater to the wash box 4. The superheater is further illustrated as provided with steam supply It; fer back-running.

.In Fig. 1, the operating connection indicated between valves I la and ma is intended to be diagrammatic, the connection being such that the opening or closing respectively of one valve by the hydraulic cylinder l'lb is accompanied by the clesing or opening respectively of the other.

Thewash box 4 is illustrated as provided with thesealing liquid supply l9 and the liquid overflow 20, which are adapted to provide a liquid seal for dippipe 21, which is connected with the pipes H and I1 leading from the generator base and superheater top respectively. The valved gastake-off 22, provided with valve 22a, leads from the wash box to the gas take-off main 23, which leads to storage, condensing and purification apparatus (not shown).

25' generally indicates a pressure storage tank for, liquefied propane, which is to be supplied in metered quantities to the carburetted water gas set as desired.

@Inaccordance with the form of the invention chosen 'for illustration, liquefied propane is caused to flow from the storage tank 25, through pipe'2B to a phase separating vessel 21 in response'to' a pressure differential therebetween. If desire'jd, pipe'26 may be provided with either the hand operated throttling valve 28, or the automatically operated reducing valve 29, or

both.

The function of the phase separating chamber 21 is'to cause the separation from each other of liquefied propane passed from storage through pipe'2B and propane vapor produced in transit by evaporation incidental to the drop in pressurethrough pipe 26 including valves 28 and 29, if provided. The material flows into chamber 21 in a chilled condition due to this evaporation. Propane vapor separated in chamber 27 passes byway of pipe 30, provided with valve 3|, to the gas take-01f main 23, and is illustrated as metered en route by the vapor meter32.

Liquid propane separated in chamber 27 is delivered by pump 33 ,by way of pipes 34 and 35 to the water gas set, passing through the liquid,

header 36, whichmay supply'a plurality of gas sets, and through pipe 37 to the particular water set shown, entering the top of the superheater '3, with the back-run steam, supplied through [8.

Pipe 31 may be provided with the regulating valve 38,for regulating the flow of liquid propane tothe set and with the hydraulic operating valve 39*forcontrolling the admission of liquid propane '4 thereto during the desired periods of a cycle, for example, as controlled by the usual automatic controlled machine.

Liquid meter 40 is arranged in pipe ,31 for metering the liquid propane: flowing therethrough to the gas set. 4| is a shut-off valve, the closing of which disconnects pipe 31 from the liquid header 36.

.The phase separating vessel 21 is illustrated as provided withthe float chamber 42 and with the float 43, which is operably connected with the valve 3! in the vapor line from the phase separating vessel in such manner that should the float 43 sink, due to a lowering of the level of the liquid propane in chamber 21, the valve 3| will be moved toward the wide-open position, thereby increasing the flow of vapor from chamber 21, through pipe 30, to the gas take-01f main 23. Vice versa, should float 43 rise because of the rising of the level of the liquid propane .in chamber 21, valve 3| will be moved toward the closed'position, thereby reducing the flow of Va; por through pipe 30.

The automatic reducing valve 29, which may or may not be provided as desired, isilIuStrated as 'operably connected, asby pipe 44, with chamber 27, in such manner as to be responsive to changes of pressure within the chamb er,'increas-. ing pressure in chamber'Z'l tending tomove valve 29 toward the closed position and decreasing pressure in chamber 21 tending .to move valve 29 toward the wide-openposition.

The following is given as an illustrative ex: ample of the operation .of the form of the apparatus of the invention chosen for illustration in Figure '1, bearing in mind that'its usein con-i nection with thehandling .of propane specifically and its use in connection with the specific uti-. lization of the conveyed liquidin a carburetted water gas set are purely for purposes of illus-r. tration. The invention,,in its broader aspects,.is not limited to the conveying of any particular liquid of the general character described nor to any particular utilization, treatmentor other dis-. posal of the liquid delivered.

The ignitedfuel bed 5 in generator .I alter-. nately blasted with air and steam in a cyclic operation.

During the air blasting step of thecycle, termed the blow, with valve Ha closed and the stack valve it open, air blast admitted through air supplyimeans 6 raises the fuel bed to ahigh temperature and stores heat therein. The resulting producer gas issuing from the top of .the fuel bed is burned with secondary air admitted throughair supply 8. The'burning producer gas and the resultingproducts of combustion traverse the carburetter and superheater, storing heatin the refractory liningsand checker-brick thereof and issue to the atmosphere throughthe stack" valve 16.

After the .fuel bed and the. carburetterand; superheater have been .raisedto the desired .tem peratures, the blow is terminated, the

water gas generating period termed the run? is,

begun. With valve 1 i remainingmlosfid; steam, is admitted-to the base or thegeneratqr through steam supply I, for reactionwith the, ignitediuel: bed to produce water gas. The resulting up-. run water gas passes from the top of the-fuel bed through connection Ill to the carburetter, thence through connection (4 tothe superheater,

The stack valve I6 is closed shortly after the.

beginning of the steaming operation, that israfterthe up-run water gas has purged'through the' 5. stack, the combustion products of the air blast remaining in the set at the end of the air blasting operation. After this purge with valve 11a in pipe I! open, the up-run gas passes through pipes l1 and 2| to wash box 4 and thence through take-ofi 22 and valve 22a to take-off main23.

During the up-run, the blue water gas pass-- ing through the carburetter and superheater is carburetted with oil gas produced by-spraying.

oil into the top of the generator through oil supply 9 and/or into the top of the carburetter through oil supply 13, the heat stored during the "blow serving to vaporize the oil and to crack theresulting oil vapors in the presence of the blue water gas and excess steam from the generator.

After the up-run, the admission of steam through supply I is ceased and the valves Ila and Ila are reversed. Steam is admitted through steam supply l8 and passed reversely through the superheater, carburetter and generator, and the resulting back-run" water gas passed to the wash box by way of pipe II from the base of the generator and thence by way of connection 22 to the gas take-01f main 23.

After the termination of the back-run, the valves Ila and Ila are again reversed, and a short up-run is made with steam supplied to the base of the generator through steam supply 1.

Following this up-run, the cycle is repeated,

by the initiation of another air blasting operation,

the stack valve It not being opened until the products of combustion have pushed the carburetted water gas, remaining in the set at the end of the run, out of the set through connection IT.

The foregoing description of the operation of a carburetted water gas set was chosen purely for illustration and may be widely varied.

For the purpose of conveniently increasing the output of a carburetted water gas set during periods of peak loads, it has been proposed to supplement the gas production, from solid fuel and from the conventional enriching oils, with gas produced by the vaporization and/or the vaporization and pyrolysis of liquefied normally gaseous hydrocarbons such as propane and butane.

In the embodiment of the present invention illustrated in Figure 1, during the back-run, liquid propane is pumped from the phase separating chamber 2'! by pump 33 through pipe 35, liquid header 36, liquid meter Wand pipe 3'1 into connection I! in the proximity of the superheater top, to which the steam is simultaneously admitted through steam supply '23. The result;

steam and gas resulting from the pyrolysis of the propane vapor, pass through the back-run pipe I] to the wash box 4 and thence to the gas takeofi main 23. V

Simultaneously the vapor phase propane separated in the phase separating chamber 2! may be passed by way of pipe 39, valve 3|, and the'vapor meter 32 into the gas take-off main 23, serving as cold enrichment of the gas produced in the set.

At the end of the back-run, the carburetter and superheater are full of propane vapor resulting from the evaporation of .theliquidpropane f.

cracked by passage through the fuel bed. zi Ihis .1 vapor'phase propane is pushed through. the wash box into the gas take-off main by the succeeding up-run gas, and also serves as enrichment.

According to the embodiment of the invention illustrated in Figure 1, the mixture of liquid and vapor. phase propane, produced by the evaporation due to drop in pressure as the liquid propane flows from storage tank 25,-isseparated into the respective liquid and vapor phases in chamber 21. The separated liquid phase ispumped by pump 33 through the liquid meter 40 under a sufhciently elevated pressure .sothat'when the liquid propane passes through the liquid meter the. temperature of the propane is below its boiling point under said elevated pressure.

In case the liquid phase material is a mixture,

the. pressure at the liquid meter is preferablysuch that the temperature obtaining is below the boiling point ofathe lowest boiling constituent thereof. v

The pressure is preferably such as to preclude the presence of any substantial proportion, by-volume, of vapor phase with'the separated liquid material as it passes through said-liquid meter, in spite of any pressure drop or rise of temperature which may occur between thezpump and the liquid meter. I

Since the evaporation of a portion of the liquid propane. due to pressure drop in the passage from the storage tank to the phase separating chamber abstracts heat from the remaining liquid phase material. reducing its temperature, the pressure developed by pump 33, therefore,

need only be sufilcient to maintain the chilled liquid in the liquid phase up to and through the liquid meter as described.

In the apparatus illustrated in Figure 1, connection 28 leading from the storage tank to the phase separator is shown provided with a hand operated throttling valve and with an automati-- cally operated reducing valve. Either or both to produce a selected pressure drop in line 26,- and the automatically operated reducing valve may be desired to maintain a constant pressure drop therein.

As stated, however, either or both of these valves may be omitted. In the absence of reducing valve 29 and its operating connection 44, any loweringof the level of the liquid in chamber 21 moves valve 3| toward the wide-open position, and by bleeding vapor from chamber 21 reduces the pressure therein, which in turn increases the difierential pressure between the storage tank and the chamber 21, thereby increasing the flow of material through line 26 to restore the liquid level in chamber 21. Any increase in the height of the liquid'level in chamber 2! is accompanied by the reverse operation of the float 43 and valve 3!, which increases the pressure in chamber. 21, which in turn reduces the pressure diiferential between: tank 25 and chamber 21, thereby reducing the flow through line 26 to restore the liquid level in the chamber. I

By proper selection of pressure conditions in chamber 21, with respect to other conditions obtaining, including the supplying of heat to the liquid from the atmosphere or otherwise, if required, any desired proportion of-the materialpassed from storage may be evaporatedand'bled off from the chamber as vapor through connection 30. The proportion of vapor phase thus formed and separated may preferably be a minor portion :of' the material leaving storage. but if desired theimajor portion may be thus :separated aswapor phase material, a minor portion being passed .asliquid through .the liquid meter. With commercial liquid propane, up to approximately 5.0% of the liquid :may be evaporatedibyexpansion downrto atmospheric pressure without requiring the supply of extraneous heat. Since "with the evaporation ;of :any considerable proportion of the liquid, the temperature of the remaining liquid will be reduced well below the ambient temperature, heat for further evaporation may be conveniently supplied from the atmosphere.

=I-n many :cases.zsu.ch as inzthe'use 'of theinvention particularly described, after the separated liquid phase material has beensmetered thereis no need to inhibit the vaporization thereof. In the. use. of liquefied normally gaseous .hydrocarbons, such as hydrocarbons of from :3 to 4 carbon atoms per molecule, the manufacture of combustible gas the liquefied hydrocarbon-material is. to be vaporizedinthe process in :any event.

The invention usefully employs "the'evaporation of a portion of theliquefied-hydrocarbon material to: permit the, conveying of the remainder in liquid phase to the proximity of the zone of .its utilization and its accurate metering.

The vapor phase material separated in chamber-.21, may also beaccurately metered prior to use. If desired, baffles or other phase contacting means, such for example as rfactionating column. packing, may :be employed if desired-to remove entrained. liquid phase material from the separated vapor phase prior to the metering of the, latter.

As a. specific example of the-operation of the invention, liquefied propane in .-a storage tank under a temperature --of about 30 F. and .nnder a. pressure of about 100 pounds-per square inch absolute pressure and having an enthalpy of about 123 B. t. u. per pound is passed through a line 4 inches in diameter to a phaseseparating chamber with a pressure drop en route of about 440 pounds per square inch, with anevaporation of about of the material and a drop in temperature to about -1- F.

The separated vapor phase material is bled-off to.-.the gas take-on main serving-six carburetted Water .gas. sets.

The separated liquid-phase material-is pumped by a booster pump under an increase in pressure of about. 50- pounds .per square inch through a linchline-about 200 it. long and thence through six-2 inch lines about 1.00 it. long to six-liquid meters, under ambient temperature conditions oiabout 120? F., the-metered material-going to thesi-x Bil-rt. diameter water gas sets during. the back-mun periodof the .cycleoteachset.

Approximately mgallonsof propaneper cycle issupplied to each of theisix sets with about 1-10. cyolesperhour. About65% of the propane suppliedis reformed by passagethrough the :fuel beds iofnthe generators of the respective sets, being supplied thereto during the back-run" with the back-run steam to the super-heater topsot the several sets. Abo ut.35 of the propane is .used as *enrichment" not :being-reformed, including propane vapor remaining in thegenerator top, carburetter and "superheater at theend of the: back-run as wellas the separated vapor phase material bled :into' the gas take-off main.

finder the increased pressure supplied .by the :pump, :the ambient temperature .at the liquid: :meter :is well. below the boiling point or 8 the liquid :propane :being metered, and no sub stantial volume of vapor phase material .is :presout to impair the accuracy of-the metering taper-- ation.

i In the employmentof the invention-in connection with'the operation of a considerable number ofcarburetted water gas sets, due to staggering of the cycles of the individual gas sets, pump 33 may be continuously pumping separated liquid phase hydrocarbon material from the separator 2 to the liquid header 36, the liquid flowing therefrom continuously through at least one liquid meter. In a case in which the invention is employedin connection with the operation of only one carburetted water gas set, the ,flow of liquidhydrooarbon material from thephase separator 21 through thev liquid meter will normally be discontinuous, the. flow taking place during only a certain period or periods in the gasmaking cycle. In such case, the refrigeration and the repressuring of the separated liquid phase material should preferably be such as to maintain the material in the line from the pump to and through the liquid meter in liquid phase during the period or periods of the cycle in which there is no flow of material through line 35. In using the invention in-connection with the operationofonly a few water ,gas sets, the nowof liquid material from pump 33 may likewise :be discontinuous, although not to such arr-extent as in the case of the operation of only one gas set and therefore the same, considerations may apply but to a lesser degree.

Referring to Figure .2:

This .figure illustrates another form of the invention. ,Pipelflfl leads from a storage tank (not shownl, which may be similar to tank 25in Figure 1 containing. liquid propane, under the pressure resulting from storage under atmospheric temperature conditions.

The liquid propane passes through pipe Hill to the heat exchanger [01 in response to pressure differential therebetween.

The heat exchanger is "illustrated as provided with upper and lower tube sheets I02 and I03 respectively and with the tubes I04 extending therebetween.

The liquidpropane containing some vapor, produced due to; pressure dropin pipe I00, enters the heat exchanger by way of the space above the upper tube. sheet and flows downwardly through thetubes and thence by 'wayof the space below-the lower tube sheet, the connection H15, liquid -meter H116, and connection 101, to a car-' buretted water gas set (not shown). For example, the utilization of the liquid propane in the gas manufacturing apparatus may 'be asshown anddescribed'in connection with Figure 1,

The flow-of the liquid propane from storage to valve .0, the resulting chilled vapor, passing into the-lower portion of the space between the tube sheets of heat exchanger HH, and back and forth between bafilessuch as Hlla, cools the mixture-of :liquid propane and propane vapor I passedintozthe heat exchanger above the upper tube sheet.

This results in .the condensation- IIII is provided with means for adjusting its opening, and in operation suflicient liquid propane is expanded therethrough, to reduce the temperature of the liquid propane issuing from the base of the heat exchanger, sufficiently low as to ensure the absence of any substantial.

volume of vapor phase therein during metering;-

The propane vapor bled off through expansion valve I I0, passes out of the heat exchanger by way of connection III, and is passed through the vapor meter II2, from whence it passes, by way of connection H3, to the gas take-off main II I, which may be connected to one or more gas sets (not shown) in similar manner to take-off main 23 in Figure 1.

Expansion valve IIEI is illustrated as operated by hydraulic cylinder H5, which may be actuated by the automatic control machine (not shown) of the carburetted water gas set, so as to be moved toward the wide-open position simultaneously with the opening of valve H13, in line II".

If desired, the operation of valve III} may be arranged so that it does not entirely close, thereby bleeding oii through the valve a small proportion of propane, to provide refrigeration in the heat exchanger during periods of the water gas cycle when valve I08 is closed. To reduce loss of refrigeration the heat exchanger is illustrated as lagged with the heat insulating material H6.

In the form of the invention illustrated in.

Figure 2, the vaporization of an additional proportion of the liquid propane permits the omission of the step of repressuring the liquid propane prior to passage through the liquid meter. If the additional vapor cannot be conveniently utilized, as for cold enrichment as described, any desired proportion oi the vapor leaving the heat exchanger may be compressed, after cooled and returned to storage as liquid. The same procedure may be followed, if desired, in the case of any proportion of the separated vapor phase material from the phase separator of Figure 1.

Referring to Figure 3:

Figure 3 shows the upper portion of the apparatus of Figure 2, modified somewhat to provide for the periodic removal of uncondensed gas from the upper portion of the heat exchanger should such gas tend to accumulate.

As in Figure 2, I indicates the pipe leading from the liquid propane storage. IIJI is the heat exchanger generally. IE2 is the upper tube sheet, I04 the tubes, IIOa a baille, and He the insulating lagging of the heat exchanger. III is the vapor line leading through vapor meter H2 and connection I I3 to utilization of the vapor, such as by admission to the gas take-01f main (not shown).

In the modified apparatus of Figure 3, a bleeder connection I is provided leading from the upper portion of the space above the upper tube sheet to connection III. The bleeder connection is illustrated as provided with two valves I2I and I22 arranged in series.

Pressure actuated valve I2I is operatively connected by way of pipes I26 and I23 with the space above the upper tube sheet and is arranged to remain closed when the pressure in said space is below a predetermined value, and to open when said pressure is above said predetermined value. Valve I22 is operatively con- .10 I nected with float I24, in such manner that whe the float is maintained in its uppermost position by the liquid in the space above the tube sheet, the valve I22 is in the'closed position, but when a lower level of liquid causes a falling of the float, valve I22 is moved toward the open position. v Y

As a resultof these provisions, if a sufficient body of uncondensed gas accumulates in the top of the'heat exchanger, under the'storagepressure less the line drop, both valves will be opened and the gas automatically bled oif. Thev refilling of the space above the upper tube sheet with liquid raises the float and closes valve I22. Due to provision of valve I2I pressure inthe topof the heat exchanger will not be unduly reduced with the consequent flashing-off .of unnecessary proportions of the liquid. j f

As previously stated, the invention is capable of many other applications than the specific application particularly described above. It may readily find use in the handling andiutilization of other normally gaseous hydrocarbons .than propane and butane, such for example as ethane, ethylene, propylene, butylenes and others. Moreover, it may be applied to the handling of volatile liquids, other than hydrocarbons, such for example as methyl chloride, boiling point 24 0., methyl amine, boiling point '6.7"C., vinyl chloride, boiling point -12 C. and others.

I The invention is not limited to use with organic liquids as it may be readilyapplied to the'handling of such materials as liquid anhydrous ammonia, boiling point -33? C. and to superheated water. g

The invention is applicable to the piping and metering of liquid phase material containing two or more constituents, one or more of which may tend to separate as vapor phase from the remainin liquid material upon drop in pressure under the ambient temperature conditions. Included-is liquid phase material relatively non-volatile .at atmospheric pressure under the temperature conitions obtaining and containing dissolved material which is gaseous at atmospheric pressure under the temperature conditions obtaining and maintained in liquid phase by elevated pressure. Such liquid phase materials include, forexample, aqueous ammonia and carbonated liquids.

The invention has particular advantages in its the utilization of liquefied normally gaseous hydrocarbon material in the manufacture of combustible gas, for example, in a carburetted water gas set, as previously described and otherwise. In such use, separated vapor phase material bled off from the phase separating chamber may be very conveniently employed in the gas-making operation, as Well as the separated liquid material. This vapor phase material may be bled into the gas take-off main, as previously described, at any period in the cyclic operation of any gas set connected therewith, or maybe passed .into any set during any desired gas-making period, for purposes of enrichment with little or no cracking or to be reformed by passagethrough the fuel bed, Withcracking therein to lighter hydrocarbon material, hydrogen, and carbon.

In the claims the expressions substantial volume of vapor phase material, substantial volume of vapor phase hydrocarbon material and similar expressions are intended t mean volumes of vapor such as 'to afiect the accuracy of metering of the liquid phase material'beyond the limits of reasonable tolerance. It is obvious that from this standpoint the lower the proportion 11 201 vapor phase fin fizhe material passing through lcheiliquid :meter the :better. :Itiis likewise obvious '#that one itolerances as ;to meter :accuracy Jmay widely .as :between different uses of the :in-

wention. Preferably the proportion of yapor iphase accompanying the liquid phase material when metered should be less than "thereof zbyouolume, more preferably :should .bBIleSS than 53% fthereof, :and .still more preferably less than 1 or even 11% ithereoi. :In :the .case :of normally gaseous hydrocarbons these :proportions :repre- 35-56111 the evaporation of extremely .small proporitions by weight. The :invention, however, is :not necessarily :Iimited to the presence of any -:pa.rtlcular proportion f vapor :phase .material with rthe liquid phase undergoing metering.

. fflther 'Jnodifications may readily :occur 1110 those skilled in the art without departing from the spirit :0! :the :present invention, which is intended befiimited only as required by :the appended .-:elalms andzthe priorzart.

swesclaimz' ll. illheimethod 10f distributing normally :gasenus hydrocarbon-material employed in-the manuitac'turerof combustible :gasiby a ,process involvring alternate iheatingiof contact material in .a

sizes-generating .set and passing hydrocarbon and =ssteam ftherethrouglh in a :cyclic operation, comprising flowing said liquefied normally gaseous hydrocarbon material from iaicontainer in which :mressure conditions are :such as to maintain said momnazlly gaseous material -substantially in the illiquid :p'hase "thereinunder the temperature coniiitions obtaining, I along a confined path in which pressure conditions are reduced with respect 'to xsaildcontainer to cause flow from said container and to cause partial conversion of said liquefied :mormally gaseous hydrocarbon material to "the wapor phase \wi'th the chilling of the "remaining iliquid phase material, to a confined-phase sepasrating :zone; withdrawing vapor phase material;

flowing said chilled liquefied normally gaseous hydrocarbon material from said phase separating-zone along :a second confined path to and a'liquid meter at an increased pressure with respect to said phase separating zone such fihat the temperature of said chilled liquefied normally gaseous hydrocarbon material in said second confined path is below its boiling point thereim tl-1ereaiter passing said metered hydrocarbon material with steam through 'said -hot montact material of said gas-generating set to produce combustible gas.

2. The method of utilizing normally gaseous mydrocarbon mater-ial employed the manufac- '?bon substantially in :the liquid state therein :un-

der the -.temperature conditions obtaining, which =-comprises conducting said liquefied normally gaseous hydrocarbon along .a confined path in which mhe pressure :conditions are reduced :with reenest rte said container to cause flow from said pontainer and to cause partial conversion of said :liquefied normally gaseous hydrocarbon material ate the :vapor phase with the chilling of the remaining liquefied normally gaseous hydrocarbon 12 *materiaht .a :confined phase separating :zone; withdrawing zan'd :metering the mesultingseparated vapor iphase hydrocarhonzmaterialzso{asfto maintain approximately constant liquid zlevel in said phase separating :zone; iflowing said achilled liquefied :normally gaseous hydrocarbon :material from said :phase :separating zone along a second confined :path to :and through a .liquidmeterat an increased pressure with respect :to :said phase separating zone such :that ithe temperature of said chilledji-quefiod normally gaseous .imaterial in ZBEj-dISECOIld .confmed :path is below its boiling point therein; thereafter passing said lhydrocarbon material which was metered rindiquid phase through said heated contact material 'in the :presence "of steam during ;a gas-making period of said cycle, and mixing lWith :combustible gas thereby produced said vaporiphase'lhydroear- :bon material which was separately metered in wapor phase.

3. apparatus for distributing i'liquified normally gaseous hydrocarbon materialz in 'the manufacture-of combustible gas ina gas-making set, including asg'as-making generator adapted to contain hot contact material, said liq'uified normally gaseous :materia'l subjected, wduring :dis- :tribution, :to pressure :and temperature conditions whichcause partial :gasizfication thereof, [comprisingxa apressure storage tank, :a conduit Heading *iromcsaid rta'nk :to a confined phase separating chamber, a pressure reducing valve insa'id con- ;duit responsive to :pressurefiin said xphase separating chamber and adapted to closesaid conduit when the pressure in said phase separatingc'ham- 'ber exceeds a predetermined pressure, a second conduit-connected to the upperpartof said chamber for leading vapor "phase material therefrom, a :float adapted :to rise and fall with the devel .of the liquid in :said phase separating chamber and :operatively@connectedwith the valve-in said second conduit wlriereby said valve is moved to- -ward the closed position upon the rise *of .said liquid level :and toward the open :position upon :the fall of said liquid ileveL a third conduitcon- 'nected to the lower part of said phase-separating chamber and in fluid flow communication with said .igas-making generator, said :third conduit having a pump and a liquid meter therein, said pump being located between said phase separating chamber and saidtmeter.

1. .An apparatus "for distributing liquifiednormallygaseous hydrocarbon material in the manufacture of combustible gas in a :gas making set, includinga gas-makinggeneratoradapted to-con- 'tain hotcontact material, and gas take-off means leading to .a-qgaszstorage vessel, said iiquified 'normally gaseous material subjected, during distribution, .to pressure and temperature-condi- 'it'iODS which cause partial :gasification :thereof, comprising a pressure storage tank, -a conduit leading from said :tank to :a oonfined phase separating chamber, a pressure reducing ya lve in said conduit :responsive to pressure in -se 'id phase separating chamber and adapted to :close said conunit when the pressure said phase separating chamber exceeds a predetermined pressure, a second conduit connected 'to the upper part of said chamber for leading vapor phase material therefrom and in fluid flow communication with said gas take-off means, a vapor meter located in said second conduit, a float adapted to rise and fal-l'with the level ofthe liquid in said phase separating chamber and operatively connected with the valve in said second conduit whereby said valve is moved toward the closed position upon the rise of said liquid level and toward the open position upon the fall of said liquid level, a third conduit connected to the lower part of said phase separating chamber and in fluid flow communication with said gas-making generator, said third conduit having a pump and a liquid meter therein said pump being located between said phase separating chamber and said meter.

JOHN S. HAUG.

PRICE W. JANEWAY, JR.

REFERENCES CITED The following references are of record in the file of this patent:

Number 14 UNITED STATES PATENTS Name Date Rose Feb. 16, 1926 Huif Dec. 13, 1927 Rosenthal Apr. 12, 1932 Faber July 18, 1933 Young Sept. 25, 1934 Marden Sept. 3, 1935 De Motte Mar. 3, 1936 Young Sept. 22', 1936 Werts May 6, 1941 Benz et a1 Aug. 4, 1942 Hirsch Dec, 29, 1942

Claims (1)

1. THE METHOD OF DISTRIBUTING NORMALLY GASEOUS HYDROCARBON MATERIAL EMPLOYED IN THE MANUFACTURE OF COMBUSTIBLE GAS BY A PPROCESS INVOLVING ALTERNATE HEATING OF CONTACT MATERIAL IN A GAS-GENERATING SET AND PASSINNG HYDROCARBON AND STEAM THERETHROUGH IN A CYCLIC OPERATION, COMPRISING FLOWING SAID LIQUEFIED NORMALLY GASEOUS HYDROCARBON MATERIAL FROM A CONTAINER IN WHICH PRESSURE CONDITIONS ARE SURE AS TO MAINTAIN SAID NORMALLY GASEOUS MATERIAL SUBSTANTIALLY IN THE LIQUID PHASE THEREIN UNDER THE TEMPERATURE CONDITIONS OBTAINING, ALONG A CONFINED PATH IN WHICH PRESSURE CONDITIONS ARE REDUCED WITH RESPECT TO SAID CONTAINER TO CAUSE FLOW FROM SAID CONTAINER AND TO CAUSE PARTIAL CONVERSION OF SAID LIQUEFIED NORMALLY GASEOUS HYDROCARBON MATERIAL TO THE VAPOR PHASE WITH THE CHILLING OF THE REMAINING LIQUID PHASE MATERAL, TO A CONFINED PHASE SEPARATING ZONE; WITHDRAWING VAPOR PHASE MATERIAL FLOWING SAID CHILLED LIQUEFIED NORMALLY GASEOUS HYDROCARBON MATERIAL FRON SAID PHASE SEPARATING ZONE ALONG A SECOND CONFINED PATH TO AND THROUGH A LIQUID METER AT AN INCREASED PRESSURE WITH RESPECT TO SAID PHASE SEPARATING ZONE SUCH THAT THE TEMPERATURE OF SAID CHILLED LIQUEFIED NORMALLY GASEOUS HYDROCARBON MATERIAL IN SAID SECOND CONFINED PATH IS BELOW ITS BOILNG POINT THEREIN; THEREAFTER PASSING SAID METERED HYDROCARBON MATERIAL WITH STEAM THROUGH SAID HOT CONTACT MATERIAL OF SAID GAS-GENERATING SET TO PRODUCE COMBUSTIBLE GAS.

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