US2630191A

US2630191A - Cyclic adsorption process

Info

Publication number: US2630191A
Application number: US155956A
Authority: US
Inventors: Ernest B Miller
Original assignee: JEFFERSON LAKE SULPHUR CO
Current assignee: JEFFERSON LAKE SULPHUR CO
Priority date: 1946-10-28
Filing date: 1950-04-14
Publication date: 1953-03-03
Anticipated expiration: 1970-03-03

Description

March 3, 1953 E. B. MILLER CYCLIC ADSORPTION PROCESS 9 Sheets-Sheet 1 Original Filed Oct. 28, 1946 INVENTOR. 55: fl llY/e .B W *M fiTTO PNEYS March 3, 1953 E. B. MILLER 2,630,191

CYCLIC ADSORPTION PROCESS 9 Sheets-Sheet 2 Original Filed Oct. 28, 1946 P IL LE:

V INVEN EB./V/I' r- %M7LM ATTORNEY March 3, 1953 Original Filed Oct. 28, 1946 E. B. MILLER CYCLIC ADSORPT ION PROCESS 9 SheetsSheet 4 March 3, 1953 4 E. B. MILLER 2,630,191

CYCLIC ADSORPTION PROCESS Original Filed 001;. 28, 1946 l 9 Sheets-Sheet 5 INVENTOR. E6, AZV/er March. 3, 1953 E. B. MILLER CYCLIC ABSORPTION PROCESS Original Filed Oct. 28, 1946 9 Sheets-Sheet 6 K////////////////////////;/fi

E :1. E1. 1 l

INVENTOR. 35 13, Af/l/er M ,l-M

ATTOBAEYS March 3, 1953 9 Sheets-Sheet 7 Original Filed Oct. 28, 1946 INVENTOR.

ATTORNEY 9 Sheets-Sheet.- 8

Original Filed Oct. 28, 1946 INVENTOR. 15. Z3, M ///e I" March 3, 1953 E. B. MILLER 2,630,191

CYCLIC ADSORPTION PROCESS Original Filed 001;. 28, 1946 9. Sheets-Sheet 9 LEI-E715- frite.

Patented Mar. 3, 1953 GYCLIC ABSORPTION PROCESS Ernest B. Miller, Houston, Tex., assignor to Jefferson Lake Sulphur Company, New Orleans, La., a corporation of New Jersey Original application October 28, 1946, Serial No. 706,108. Divided and this application April 14,

" 1950, Serial No. 155,956

7' Claims. (Cl; 183-1142) 1 This invention relates to gas dehydrating and has more particular reference to a novel and continuous method of removing moisture and condensable hydrocarbons from wet natural gas at the source, prior to the transmission thereof through pipe lines and recovering the condensable hydrocarbons.

Natural gas transmitted through pipe lines always contains moisture. This moisture forms crystalline hydrates, which clog the pipe lines and valves. Heretofore, the moisture has been removed from the gas at the point of entrance to the pipe lines by using different types of adsorbents, principally activated alumina and fluo- The gas is usually pumped through large cylinders filled with the adsorbent material and the material is intermittently reactivated by cutting off the flow of gas and utilizing either heated air or gas. This requires the use of at least two adsorption units, including complicated control esuipment, for directing the flow of wet gas through either unit.

Thus far, no attempt has been made to recover any gasoline as a \by-product of the dehydration method. In fact, the usual adsorbents employed, such as alumina and fluorite, are not sufficient for this purpose because the size of their pores is too large.

One of the objects of this invention is to provide a novel method of dehydrating wet gas under high pressure using an adsorbent, such as silica gel, and recovering a large percentage of the condensable hydrocarbons, such as gasoline, etc.

Another object of the invention is to provide a novel method of recovering condensable hydrocarbons from wet natural gas under high pressure which is characterized by moving a series of separated layers of adsorbent material in a hot gas as it passes therethrough and condensing the'vaporized hydrocarbons and separating them from the hot gas after its passage through the adsorbent material.

Another object of the invention is to provide a novel method of dehydrating wet natural gas under high pressure and-recovering condensable hydrocarbons therefrom as characterized above wherein the gas to be treated is directed in succession through the adsorbent material'at at least two points in its closed path.

Another object of the invention is to provide a novel method as characterized above wherein the flow of the gas to be treated through the adsorbent material is counter-current to the flow of the hot gas therethrough. 5 Other objects and advantages of the invention will appear in the specification, when considered in connection with the accompanying drawings,

in which:

Fig. 1 is a side elevation showing the mountin and arrangement of the apparatus of this 'invention;

Fig. 2 is a plan view of the apparatus shown in Fig. 1;

Fig. 3 is a plan view of the dehydrater;

Fig. 4 is a side elevation, partly in section, of the dehydrater driving mechanism;

Fig. 5 is a vertical sectional view of the dehydrater, taken on the line 5-5 of Fig. 3, but omitting the driving mechanism;

Fig. 6 is a horizontal sectional View of the dehydrater, taken on the line 6-6 of Fig. 5, but drawn to a smaller scale. i

Fig. '7 is an enlarged vertical view of the seal shown in the upper manifold of Fig. 5;

Fig. 8 is an enlarged plan view of the seal shown in the upper manifold of Fig. 5;

Fig. 9 is a vertical sectional view, taken the line 9-9 of Fig. 8;

Fig. 10 is a horizontal sectional View of the dehydrater, taken on the line l!!lil of Fig. 5;

Fig. 11 is a partial vertical sectional view of a manifold, showing the details of a roller;

Fig. 12 is a plan view of a cylindrical adsorbent containing unit;

Fig. 13 is a vertical sectional view, taken on the line |3-l3 of Fig. 12;

Fig. 14 is a schematic view to show the flow of wet gas through the first and second dehydration steps, and the flow of hot gas through the activation stage and the condenser and separator; and

Fig 15 is a schematic view to show a modification of the flow of hot gas through the activation stage and the condenser and separator.

This application is a division of my co-pending application, Serial No. 706,108, filed October 28, 1946, for Apparatus for Dehydrating Gas and Recovering Condensable Hydrocarbons Therefrom. now Patent No. 2,507,608.

The present invention is drawn to a novel method of dehydrating wet natural gas under high pressure and recovering the condensable hydrocarbons therefrom. While any suitable apparatus may be employed in carrying out the novel method of the present invention, for the purpose of illustration, the novel method will be described as employing the apparatus shown and described in my aforesaid co-pending application.

Referring now to the drawings, there is shown in Figs. 1 and 2, one embodiment of apparatus and the arrangement thereof for carrying out the method of this invention. The apparatus shown includes a three-stage, dehydrater l,.the first and second stages ofwhich are used' to dehydrate the wet gas, the third stage being used to reactivate the adsorbent material within the dehydrater; an intercooler 2, employed ,tocool the;

wet gas between the first and second dehydratiorr stages; a heater 3 employed to heat the gas I a used in the, reactivating stage of: the dehydrater; a condenser 4 employed to, condense the moisture from; the heated gasafter it has passed through the reactivation stageof thedehydrater; and a.

separator 5 employed to separate thecondensate from the gas. The dehydrater, cooler and condenser are preferably supported in. a raised positionby a suitable framework, indicated generally at 6.

The wet'gas-is delivered, at high pressure, from the usual compressor or source of supply (not shown), to the first stage of the dehydrater by means of a pipe line I. After passing through the first stage of the dehydrater, during which passage some of the moisture was removed, the

now partially dried gas passes through, a pipe line 8' into the intercooler 2. From the intercooler, the cooled, partially dry gas passes through apipe line 9 into the second stage of the dehydrater, where, it is completely stripped of its remaining moisture. From the second stage, the now dry gas passes into a pipeline I for transmission to the points of use.

A portion of the wet gas is diverted from the supply pipe line 1, by means' of a pipe line II, through the heater 3, where its temperature is raised to from 300 F. to 600 F., depending upon the moisture content and the type of hydrocarbons to be recovered, and, from the heater,

passes through a pipe line 12 into the third or reactivation stage of the dehydrater. The heated gas; passes through the third stage; vaporizing and stripping the accumulated moisture and. hydrocarbons from the adsorbent. Theheated gas andits vapors stripped from the adsorbent-pass throughapipeline [,3 into the condenser 4, where the vapors are condensed; from the condenser, the gas and its condensates pass through a pipe line [4 into the separator in which thecondensate is separated from the gas. The separator is provided with a drain. l5 for removing the water: and hydrocarbons. The now cooled gas in the separator passes through a pipe line [6 back into the supply pipe line I, where it mixes with the incoming wet gas on the way to the first stage of the dehydrater. The process is continuous.

The details of construction of the dehydrater l are shown in Figs. 1 to 13- inclusive. There is showna cylindrical pressure vesel ll comprising an upper shell or cap [8 having an annular flange l9 welded thereto. anda lower shell having an annular flange 2i welded thereto. The two shells are fastened together with their flanges forming a gas-tight joint, by means of bolts 22.

The vessel I1 forms a gas-tight housing for the adsorber unit and is capable of withstanding pipe line pressure.

The adsorber unit includes a rotatable annular drum 23' mounted within. the vessel 11 and fixedly attached, by means of upper and lower plates 24, 25, to a central vertical shaft 26 journalled in a stufling box bearing 21 formed in the upper shell or cap I8 and a step thrust bearing 28 secured to the bottom of the lower shell 20. A platform, 29 for supporting the mechanism for rotating the drum is mounted on the cap [8,.

The driving mechanism includes a shaft 30 connected tothe upper end of shaft 26 by a coupling 3|. The: shaft 30 is driven by suitable reduction gearing mounted in a housing 32, the reduction. gearing being driven by a motor 33 by means of belting 34 (see Figs. 3 and 4).

The rotatable annular drum 23 includes, two spaced

concentric cylinders

35, 36 which form the sidewalls of the drum (see Figs. 5 and 6). Two spaced concentric

annular plates

31, 38, each secured to the top of the

cylinders

35, 36, respectively, form the top of the annular drum, the space between the

annular plates

31, 38 forming a continuous annular opening 39 in the top of the drum. Two spaced concentric

annular plates

40, 4!, each secured to the bottom of the

cylinders

35, 36, respectively, form the bottom of the annular drum; the space between the

annular plates

40, 4| forming a continuous annular opening 42 inthe bottom of the drum.

The rotatable annular drum 23 is divided into a plurality of compartments 43 by radial partitions 0r diaphragms 44. In each of the radial compartments 43, near the bottom thereof, there is provided a plate 45 attached to the walls of the compartment, as by welding, to form a gastight joint. Each plate 45 forms a support for an elongated, foraminous, annular adsorbent container 46, which comprises two concentric tubular wire screens 41, 48 (Figs. 12 and 13), held in spaced relation by a plurality of longitudinal radial fins 49, with the annular space between the screens closed at the bottom. The mesh of the screens is such as to retain a granular adsorbent 5D in the annular space between the screens. The adsorbent employed may be any adsorbent having characteristics substantially like silica gel or the gel of other activated. hydrous oxides. Preferably, silica gel is used. Each container 46 is closed at its top by means of concentric. hoops 5|, 52 mounted on the

concentric screens

47, 48 and a. cover plate 53 detachably connected to the inner hoop 52. An annular fin 54 is secured to the cover plate 53 and projects downwardly between the hoops 5|, 52, all as shown in Figs. 12 and 13, the construction being such that, as the silica gel settles down, leaving a space between the top portion of the wire screen devoid of silica gel, the fin 54 will prevent gas from passing through the space devoid of silica gel.

Each container 46 has its bottom end detachably mounted on a hollow cylindrical hub 55 projecting upwardly from an opening formed in the plate 45, as clearly shown in Fig. 5. The hub 55 is secured in the opening 56 in the plate 45, as by welding, to form a gas-tight joint. Top and

bottom manifolds

51, 58 are mounted on the top and bottom of the annular drum 23 and close the annular openings 39, 42' formed in the top and bottom of the drum. The top and bottom manifolds are identical in construction.

.5 Each is formed in the shape of an annular trough having an annular top (or bottom) 59 and

annular side walls

60, 6|.

A plurality of compression springs 62, mounted on brackets 63 suitably secured to the inner walls of the vessel I1, yieldably press the top and bottom manifolds against the top and bottom, respectively, of the annular drum. The top and bottom manifolds are held stationary relative to the rotation of the annular drum by means hereinafter to be described and, to prevent the escape of gas between the rotating drum and the manifolds, sealing ring gaskets 64 are placed at the junction of the side walls of the manifolds and the drum. The sealing ring gaskets 64 are held in tight sealing engagement with the top and bottom of the drum by means of annular hoops 65 (see Fig. '7) which engage the gaskets and hold them against the side walls of the manifold. The upper (or lower) ends of the hoops 65 are secured to the top (or bottom) the lower portions of the hoops and side walls.

The ring gaskets 64 are yieldingly held in engagement with the top and bottom of the drum 23 by means of a plurality of compression springs 51 mounted on stud bolts 68 secured to the top (or bottom) of the manifolds and engaging annular plates or members 69 mounted on the top (or bottom) of the ring gaskets, all as clearly shown in Fig. 7.

At three circumferentially spaced points in the top and bottom manifolds, there are located seals which, by reason of the sliding contact of the radial partitions 44 against the under surface of the bottoms of the seals, divide the manifolds and drum into three sectors, each sector gas-tight with respect to the adjacent sectors. The seals are identical in construction and the details thereof are best shown in Figs. '7, 8 and 9. Each seal includes a bottom or sealing plate mounted within the manifold between spaced radial partition walls H, l2. The bottom plate 10 is yieldingly urged against the top (or bottom) of the drum and rests on the concentric

annular plates

31, 38 which form the top of the drum (or

plates

40, 4| which form the bottom of the drum), as shown in Fig. 7. The side edges of the plate are bifurcated, as shown at 13, M for the reception of gasket strips 15, i8 which are yieldingly pressed outwardly against the partition walls 11, I2 of the seal by leaf springs ll, 18, as shown in Figs. 8 and 9.

The means for yieldingly pressing the bottom plate 10 of the seal against the top (or bottom) of the drum comprise a plurality of compression springs 19 mounted on projections 89, formed on the upper surface of the plate 10. The springs 19 engage the top (or bottom) of the seal and are held in position by bolts 8| projecting through the top (or bottom) of the seal and the coiled springs and threaded into the projections 80 formed on the plate 70.

Each radial partition or diaphragm M has a portion of its top and bottom edges extending upwardly between the edges of the openings in the top and bottom of the drum. A gasket 82 is secured on these portions and extends above (or below) their top (or bottom) edges and engages the uncler face of the bottom plate 10 of the seal.

Plates 83 are secured to the tops and bottoms of the partitions and are held spaced therefrom by a spacer strip 84, the plates and spacer strip being secured to the partitions by bolts 85. The gaskets 82 are confined between the partitions and the plates 83, as by means of bolts 86, and are pressed upwardly (or downwardly) against the under surface of the bottom plates 10 of the seals by means of leaf springs 81, all as shown is Fig. 9.

In order to prevent the gaskets 82 from being unduly pressed upwardly when the gaskets are not engaging the bottoms of the seals, means are provided for spanning the reaches of the manifolds between the seals. These means comprise spaced pairs of

curved plates

88, 89 which extend between and are secured to the partition walls of the seal, as shown in Fig. 10. The bottom surfaces of the

plates

88, 89 are in the same horizontal plane as the bottom surfaces of the bottom plates 10 of the seals, as shown in Fig. 5, so that. as the gaskets 82 move out of engagement with the bottom plate of the seal, they immediately engage the

plates

88, 89.

A plurality of rollers 99 are mounted within the top and bottom manifolds. These rollers are circumferentially spaced within the manifolds and are adapted to engage the annular plates 31, which form parts of the top and bottom, respectively, of the rotatable drum. These rollers are adapted to prevent frictional surface engagement between the side walls of the manifolds and the top or bottom of the drum. These rollers are identical in construction and mounting and each comprises a threaded stud bolt 9| screwed into the side wall 6! of the manifold; a ball race 92 fixedly mounted on the bolt and a wheel 93 mounted on the ball race, all as shown in Fig. 11.

Three elbow-shaped pipes or

conduits

94, 95, and 96 having threaded ends project through the cap of the vessle I! and have their threaded ends secured to the top plate of the top manifold by means of lock nuts 91 (Fig. 5), which form gas-tight joints. The pipes are welded to the cap and hold the top manifold stationary relative to the rotation of the drum. The three pipes are circumferentially spaced with respect to the top manifold and each is secured to and communicates with the manifold at a point located between the seals.

Three

additional pipes

98, 99 and H30. having threaded ends, proiect through the bottom of the vessel l1 and have their threaded ends secured to the bottom plate of the bottom manifold by means of lock nuts l0! which form gastight joints. These pipes are welded to the bottom of t e vessel l1 and hold the bottom manifold stationary relative to the rotation of the drum. These pipes are circumferentially spaced with respect to the bottom manifold and each is secured to and communicates with the manifold at a point located between the seals. The width of the seals with respect to the radial compartments 43 containing the adsorbent units is such that at all times at least one of the partitions or diaphragms 44 is engaging the bottom plate 1!) of the seal in gas-tight engagement. As clearly seen from the foregoing. the manifolds and drum are divided into three gas-ti ht sectors by the engagement of the radial partitions or diaohragms with the seals.

As the drum carrying the annular adsorbent containers rotates, thev are continuouslv and successively moved through the three sectors, called, for convenience, the first stage, the sec- 0nd stage, and the. activation stage. The three elbow-shaped.

pipes

94, 95, and96 are connected totpipe lines I, 9. and I3, respectively; and the three

pipes

98, 99, and 100 are connected to pipe lines 8,. I0 and I2, respectively, by means of which the wetgas and hot gas flow intoand through the dehydrater.

The fiowof wet gas through the first and seconddehydration stages and the flow of hot gases through the activation stage is schematically shown in Fig. 14.

The wet gas from which moisture and hydrocarbons are to be removed is supplied under high pressure by'pipe line I and enters the top manifoldof the first stage through pipe 94. Then it moves downwardly. from the manifold, through the, opening in the top of the drum into the various compartments-of the drum, containing the adsorber, units, as are at that time contained within the; sector forming the first stage. The gaspasses-throughthe pervious layer of adsorbentmaterial, which removes part of the moisture content therefrom, into the hollow interior of the adsorber units, thence downwardly through the openings in theplates 45 into the bottom ofthe drum and through the opening therein into the bottom manifold. From the bottom manifold; the now partially dried gas passes through

pipes

98 and 8 to the intercooler 2, where it is cooled. The intercooler 2 may be of the water circulating type. From the intercooler; the gas moves through pipes 9 and 95 into the topmanifold of: the second stage. The gas moves downwardly through the second stage, in a manner similar to its downward movement through the first stage, into the bottom manifold of: the second stage, the remainder of the moisture content of the gas being-removed during its passage through the second stage.

Fromthe bottom manifold of the second stage, the now. dried gas moves through pipes 99 and Ho the various points of use.

The removal of moisture and hydrocarbons from the adsorbent material carried by the annular adsorber units is effected in the activation stage.

A portion of the incoming wet gas is diverted from the supply line I by means of a pipe line II, through the heater 3, where its temperature is raised to from 300 F. to 600 F., depending upon the moisture content and the type of hydrocarbons to be recovered. From the heater, the heated gas passes through pipe lines I2 and I00 into the bottom manifold of the activation stage. From the bottom manifold, the hot gases pass through the opening in the bottom of the drum into the bottom of the various compartments of the drum as are at that time contained within the sector forming the activation stage, thence upwardly through the openings in the plates 45 and up into the hollow interior of the annular adsorber units, through the pervious solid layer of adsorbent material into the compartments of the drum. As the hot gas passes through the adsorbent material it removes the moisture andhydrocarbons therefrom. The hot, moisture-hydrocarbon laden gas then passes upwardly through the opening in the top of the drum into the top manifold. From the top manifold, the hot gas passes through pipe lines 96 and I3 to the condenser 4, where the moisture and hydrocarbons are condensed, The now cooled gas and the condensate pass from the condenser throughpipe line I4 to the separator 5, where the condensate, isv separated from the 8 gas. The water and hydrocarbon are drained from the bottom of the separator by means of drain line I5.

From the separator the gas passes through pipe line I5 back into the supply line I, where it is mixed with the incoming gas on the way to the first dehydration stage. The process is continuous.

The chief purpose in mounting the annular drum and manifolds within the pressure vessel is to permit the equalization of pressure within the drum, manifolds and vessel, thereby permitting the drum and manifolds to be made of lighter weight material, which adds considerably to the efficient and economic operation of the dehydrator. This equalization of pressure is accomplished by means of a small opening I02 formed in that portion of the pipe line 94 within the vessel 11. And too, due to the unequal temperature of the gas as it passes through the various sectors, thereby resulting in unequal expansion of the parts of the drum and manifolds, it is considered desirable to provide each of the six

pipes

94, 95, 96, 98, 99, and I00 with expansion joints I03, located a short distance from their points of connection to the manifolds. Suitable stop valves Iil4 and I05 are located in the pipe lines I and II, respectively, to provide means for controlling the flow of gas through the dehydration and activation stages of the dehydrater.

In Fig. 15 there is shown a modification of the activation cycle. This modification is an alternative to that shown in Fig. 14 and is preferably used only in cases where the quantity of condensable vapors to be recovered from the gas is quite large.

The additional apparatus shown comprises a low pressure blower I08 for recirculating the hot gas through the heater and the activation stage of the dehydrater; a pipe line ID'I connecting the inlet side of the blower to pipe line I3; and a pipe line I08 connecting the exhaust side of the blower to pipe line II. Stop valves I09 are mounted in the pipe lines I01 and I08 to permit cutting off the circulation of gas through these pipe lines when desired.

In the modification shown in Fig. 15, the circulation of the wet gas through the first and second stage of the dehydrater is unchanged. The circulation of the heated gas through the heater and activation stage of the dehydrater is modified as shown to permit the continuous recirculation of the heated gas.

A portion of the hot gas and vapor stripped from the adsorbent in the activation stage is continuously withdrawn through pipe line I3 and passes through the condenser 4 where the moisture and condensable hydrocarbons are condensed. From the condenser the gas and the condensate pass through pipe line I4 to the separator 5 where the condensate is separated from the gas. The water and hydrocarbons are drained from the bottom of the separator by means of drain line I5. From the separator the gas passes through pipe line I5 back into the supply line I, where it is mixed with the incomlng gas on the Way to the first dehydration stage.

The greater portion of the hot gas after its passage through the activation stage passes into pipe line Ill! and is recirculated by the low pre sure blower I06 through the pipe line I08 and the heater 3 back through the activation stage of the dehydrater. The process is continuous,

aes iei When the recirculating system is used the valve I04 is closed enough to force wet gas through the heater via valve I05 and pipe line H, valve I05 being used to regulate the exact quantity of such gas permitted to flow to the heater.

The raw gas fed into the actiation circuit is for the purpose of reducing the partial pressure of water vapor and condensable hydrocarbons in the activation stage, thereby facilitating the removal of such adsorbed products from the silica gel. The quantity of gases recirculated by the blower is dictated by the amount of heat required to heat up the silica gel in the activation stage and vaporize the water and hydrocarbons adsorbed therein. The valves Hi9 provide for controlling the quantities of recirculated gases. The recirculation of the hot gas through the activation stage is facilitated due to the thickness of the adsorbent in the tubular containers.

While the blower Hi6 has been described as a low pressure blower, it actually has to stand the full pressure of the system, and is low pressure only in the sense that it does not have to overcome much resistance in order to recircu late gases through the heater and activation stage of the dehydrater.

While the gas used for reactivating the ad sorbent has been shown as being obtained from the supply line i, obviously a different source could be used, as well as a different kind of gas, such as air or steam.

For this purpose a pipe line H0 having a stop valve HI mounted therein has been shown as connected to pipe line H. The pipe line Hi3 being connected to a suitable source of gas (not shown). By closing valve I05, the gas for the recirculating circuit may be obtained through pipe line H0.

Obviously, the invention is not restricted to the particular embodiments thereof herein shown and described. Moreover, it is not indispensable that all of the features of the invention be used conjointly, since they may be employed advantageously in various combinations and subcombinations.

What is claimed is:

1. In the removal of water vapor and condensable hydrocarbons from wet natural gases involving the contact of adsorbent material with the gas with resultant adsorption of the water and condensable hydrocarbons by the adsorbent material and the subsequent treatment of the adsorbent material with a heated medium to vaporize and remove the water and condensable hydrocarbons and thereby reactivate the adsorbent material forfurther contact with the natural gases, the improvement which comprises rotating a series of separated thin beds of adsorbent material directly in succession and substantially continuously relative to and through a dehydration zone and a reactivating zone; continuously withdrawing the dehydrated gas from the dehydration zone; continuously directing a flow of the gas to be treated under high pressure through said dehydration zone; continuously heating and recycling a flow of natural gas under high pressure through said reactivating zone to vaporize the water and condensable hydrocarbons contained in the beds of adsorbent therein and reactivate the beds; continuously withdrawing a portion of the natural gas from its recycling path after its passage through the reactivating zone; condensing and recovering the water and condensable hydrocarbons from the withdrawn hot gas; di recting the flow of the stripped withdrawn gas into the flow of the gas being treated before it is delivered to the dehydrating zone and continuously supplying additional natural gas to the recycled gas to compensate for the gas withdrawn.

2. In the removal of water vapor and condensable hydrocarbons from wet natural gases involving the contact of adsorbent material with the gas with resultant adsorption of the water and condensable hydrocarbons by the adsorbent material and the subsequent treatment of the adsorbent material with a heated medium to vaporize and remove the water and condensable hydrocarbons and thereby reactivate the adsorbent material for further contact with the natural gases, the improvement which comprises rotating a series of separated thin beds of adsorbent material directly in succession and substantially continuously relative to and through a dehydration zone and a reactivating zone; continuously directing a flow of the gas to be treated through said dehydration zone; continuously heating and recycling a flow of gas through said reactivating zone to vaporize the water and condensable hydrocarbons contained in the beds of adsorbent material therein and reactivate the beds; continuously withdrawing a portion of the hot gas from its recycling path after its passage through the reactivating zone; condensingand recovering the water and condensable hydrocarbons from the withdrawn hot gas; and continuously supplying additional gas to the recycled gas to compensate for the gas withdrawn.

3. In the removal of water vapor and condensable hydrocarbons from wet natural gases involving the contact of adsorbent material with the gas with resultant adsorption of the water and condensable hydrocarbons by the adsorbent material and the subsequent treatment of the adsorbent material with a heated medium to vaporize and remove the water and condensable hydrocarbons and thereby reactivate the adsorbent material for further contact with the natural gases, the improvement which comprises rotating a series of separated thin beds of adsorbent material directly in succession and substantially continuously relative to and through a succession of dehydrating zones, and a reactivating zone; continuously directing a flow of the gas to be treated in succession and in series through said dehydrating zones; continuously withdrawing the dehydrated gas from the last one of the dehydrating zones; continuously heating and recycling a flow of hot gas through said reactivating zone to vaporize the water and condensable hydrocarbons contained in the beds of adsorbent material therein and reactivate the beds; continuously withdrawing a portion of the hot gas from it recycling path after its passage through the reactivating zone; condensing and recovering the water and condensable hydrocarbons from the withdrawn hot gas; and continuously supplying additional gas to the recycled gas to compensate for the gas withdrawn.

4. The method, as set forth in claim 3, wherein the direction of the series flow of the ga being treated is opposite to the direction of rotation of the adsorbent material beds, whereby the gas being treated will make its last passage through the freshly regenerated adsorbent material beds.

5. The method, as set forth in claim 3, wherein 11 the gas used for reactivating the beds of adsorbent material is natural gas and wherein the withdrawn gas from the recycling path is directed into the flow of the gas being treated after being stripped of its water vapor and condensable hydrocarbons.

6. In the removal of water vapor and condensable hydrocarbons from wet natural gas involving the contact of adsorbent material with the gas with resultant adsorption of the water vapor and condensable hydrocarbons by the adsorbent material and the subsequent treatment of the adsorbent material with a heated medium to vaporize and remove the water and condensable hydrocarbons and thereby reactivate the adsorbent material for further contact with the natural gases, the improvement which comprises maintaining a bed of adsorbent material in each of two zones; directing a continuous flow of wet natural gas through one of said zones so that the water vapor and condensable hydrocarbons in the gas will be adsorbed by the beds of adsorbent material therein; continuously heating and recycling a flow of gas through the other of said zones to vaporize the waterand condensable hydrocarbons contained in the bed of adsorbent material therein periodically shifting the relative position of the particular adsorbent bed and the particular flow of fluid in each of said zones so that each zone becomes, in succession, a dehydration zone and a reactivating zone; continuously withdrawing a portion of the hot gas from its recycling path after its passage through the reactivating zone, condensing and recovering the water and condensable hydrocarbons from the withdrawn hot gas; and continuously supplying additional gas to the recycled gas to compensate for the gas withdrawn.

7. In the removal of Water vapor and condensable hydrocarbons from wet natural gas involving the contact of adsorbent material with the gas with resultant adsorption of the water vapor and condensable hydrocarbons by the adsorbent material and the subsequent treatment of the adsorbent material with a heated medium to 12 vaporize and remove the water and condensable hydrocarbons and thereby reactivate the adsorbent material for further contact with the natural gas, the improvement which comprises maintaining at least one bed of adsorbent material in each of a plurality of zones; continuously heating and recycling a flow of gas through one of said zones to vaporize the water and condensable hydrocarbons contained in the bed of adsorbent material therein; directing a continuous flow of wet natural gas in succession and in series through the remainder of said zones so that the water vapor and condensable hydrocarbons in the gas will be adsorbed by the beds of adsorbent material therein; periodically shifting the relative position of the particular adsorbent beds and the particular flow of fluid in each of said zones so that each zone becomes, in succession, a reactivation zone, and, in reverse order to the flow of gas therethrough, each a successive dehydration zone, whereby the gas being dehydrated will make its last passage through freshly reactivated adsorbent material beds; continuously withdrawing a portion of the hot gas from its recycling path after its passage through the reactivation zone; condensing and recovering the water and condensable hydrocarbons from the withdrawn hot gas; and continuously supplying additional gas to the recycled gas to compensate for the gas withdrawn.

ERNEST B. MILLER.

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

UNITED STATES PATENTS Number Name Date 1,528,459 Voress et a1 Mar. 3, 1925 1,948,779 Abbott et a1 Feb. 27, 1934 2,053,159 Miller Sept. 1, 1936 2,283,990 Higley May 26, 1942 2,286,920 Miller June 16, 1942 2,535,902 Dailey, Jr Dec. 26, 1950 2,541,694 Galson Feb. 13, 1951

Claims

6. IN THE REMOVAL OF WATER VAPOR AND CONDENSABLE HYDROCARBONS FROM WET NATURAL GAS INVOLVING THE CONTACT OF ABSORBENT MATERIAL WITH THE GAS WITH RESULTANT ADSORPTION OF THE WATER VAPOR AND CONDENSABLE HYDROCARBONS BY THE ABSORBENT MATERIAL AND THE SUBSEQUENT TREATMENT OF THE ADSORBENT MATERIAL WITH A HEATED MEDIUM TO VAPORIZE AND REMOVE THE WATER AND CONDENSABLE