US1074094A

US1074094A - Apparatus for liquefying gaseous mixtures.

Info

Publication number: US1074094A
Application number: US64169211A
Authority: US
Inventors: Hermann Blau
Original assignee: Individual
Current assignee: Individual
Priority date: 1911-07-31
Filing date: 1911-07-31
Publication date: 1913-09-23
Anticipated expiration: 1930-09-23

Description

H. BLAU. APPARATUS FOR LIQUEFYING GASEOUS MIXTURES.

APPLICATION IILED JULY 31, 1911.

5 Wue ntoz $5; 1 1 a Roman;

i ,into the separating vessel HERMANN BLAU, or AIJGSBURG, GERMANY.

APPARATUS FOR LIQUEFYING GASEOUS MIXTURES.

Specification of Letters Patent.

Patented Sept. 23, 1913.

Application filed July 31. 1911. Serial No. 641,692.

the following is a specification.

This invention relates to apparatus for the production of an illuminating liquefied gas, and has for its object the recovery, in the manufacture of an illuminating liquefied gas, of liquefiable constituents from the so-called permanent gases, such as hydrogenand methane, the overcoming of ditliculties heretofore encountered 1n the manufacture of an illuminating liquefied gas, increased economy and efficiency in the proccss and superiority in the product, together with other advantages hereinafter set forth.

In the accompanying drawing, forming part of this specification, is illustrated apparatus suitable for securing the objects of this invention.

Figure 1 is an elevation partly in vertical section of such apparatus. Fig. 2 is an elevation partly in vertical section of the apparatus shown in Fig. 1 with the addition of a heating coil 11.. Fig. 3 is an elevation partly in vertical section of the apparatus shown in Fig. 2 with the addition of the separating vessels D and D and the coolers W and G and their connecting pipes and means for equipping the separating vessel D so that it is a rectification column. Fig. 4 is an elevation partly in vertical section of the apparatus shown in'Fig. 3 with the addition of the compressor K and pipes and other means for employing the permanent gases, or. a part of the liquefied gas, as a coolin agent.

In t e several figures of the drawing, like letters denote like parts.

1'" isv a pipe for leading the compressed crude gases, from which easily volatile, liquid hydrocarbons have been separated from the compressor K into'the dephlegmating or separating vessel D (Figs. 1 and 2) or 2 (Fi s. 3and 4). The pipe 7' may be provide with a heating coil H in the lower part of D (Figs. 2, 3 and 4). The dephlegmating or separating vessel D may be constructed as a rectification column by equipping it with partitions, such as horizontal plates 79, which are provided with or leave alternating openings 0 along the length of the vessel D (Figs. 3 and 4).

1', is a pipe leading from D through a cologr G and into the dephlegmating vesse 1', is a pipe leading away from the to of 1 and r is'a pipe leadlng from D into the top of D and terminating in or connect ed with a hydraulic valve h.

1' ,.is a pipe leading from the lower part of D for use in filling the illuminating liquefied gas into vessels for shipment and use. D and D are separating vessels. 1, is a pipe leading from D into a lower part of D. 1 is a pipe leading from the top of D through a cooler W and into D 7', is a pipe leading from D into a higher part of 1' is a pipe leading from the top of D through the cooler G, and 1' is a ipe leading from the cooler Gr into a still higher part of D. p

r, is a pipe leading from the cooler G into the cooler-G,.

Pipe 73, connects with and leads from pipe 73, to the regulating valve V and cooler Pipe 1-,, leads from an upper part of the dephlegmating or separating vessel D to the regulating valve V and cooler G. Pipe r leads from the lower part of D to the regulating valve V and cooler G. As shown in Fig. 4, pipe 1 may lead from the upper part of D to the regulating. valve V and cooler G. g

V is a regulating valve to regulate the flow of liquefied gas from D or D through pipe 1' or through pipe 0 or through pipe 1- or the flow of permanent gases from D,,

through pipe 7 to the cooler G. c

a, v v and o, are cocks which may be employed to open and close pipes 1' 73 r and 7' respectively, and thus to permit liquefied gas to flow, through pipe r or pipe r or pipe 1 or permanent gases to flow, through pipe 1 to the regulating valve V and cooler G, when its cock is open, and to prevent such action when its cock is closed. Although the four pipes, 13,, 1' 13., and 1' are shown in Fig. 4 connected with cooler G, as will be understood from the following description, only one of the four pipes so connected, preferably 7' 7' or r is necessary to accomplish the cooling efi'ect desired.

v, is an adjustable cock and outlet with use of permanent gases as a cooling agent,

since, as will be well understood by those skilled in the art to which this invention ap pertains, there should be, as shown at 1', in Figs. 1, 2 and 3, an exit from the upper part w manent gases are'not employed as a cooling agent and for the excess of permanent gases when the permanent gases are employed as a cooling agent.

K is a compressor, which may consist of several cylinders to compress the crude gases and the evaporated or expended gases, hereinafter referred to, at different stages of compression. In the drawing, three cylin ders, k, k, and k,,, are shown for the compression of the said gases at three different stages of compression. The largest cylinder k compresses thegases at the first or lowest stage of compression. The intermediate cylinder k, compresses the gases at the sec- 0nd stage of compression, which is higher, and the smallest cylinder is, compresses the gases at the third and still higher stage of compression. Pipe T is a suction pipe, leading fro-m the cylinder is, to the cooler G Pipes r and r shown in dotted lines, are suction pipes leading from: cylinders in and 70 respectively, to the cooler G and are shown in dotted lines because, as hereinafter explained, the cooler G should, preferably, be connected only with cylinder 10,.

The arrows of'the drawing show the directions in which the-gases and liquids flow.

temperature, and, besides'that, it makes use especially of the fact that theeasily volatile liquid hydrocarbons whichare contained in the crude gas can dissolve other gases which quality increases with increasing pressure. Those permanent gases whichare not dissolved in the liquid gas are separated out and gather above the compressed andliquefied gases; these permanent gases still contain a certain quantity of liquefiable gases. Nevertheless, this process is operated with comparatively small losses of liquefiable constituents and, besidesiathat, these losses can be decreased by increasing the pressure used for compression, or by adding-to the compressed crude gas a certain quantity of easily volatile hydrocarbons of gasdissolving quality, or by leading the permanent gases which carry liquefiable gases, while under pressure, through an absorbing liquid,

- using, preferably, the counter-current prin-.

of D for the permanent-gases when the pernew crude gases.

constituents with gas-dissolving qualities critical temperature is above the normal ciple, whereby liquefiable gases or constituents are absorbed or dissolved. The absorbing liquid'dissolves mainly the liquefiable gases. Thereafter the gases dissolved in the absorbing liquid are released by allowing the liquid, which is saturated with gases,

to pass out under the pressure of a suction-- pipe of the compressor, the p'ressureof the suction-pipe being relatively lower, and then the released gases are sucked into the compressor again and compressed together with Experience in the practical use of the liquefied illuminating gas made according to the method just described has shown, however, that it is advisable 30 not to take the easily volatile liquid hydrocarbons, which are contained in the crude gas, intothe gas to be liquefied, or, at the utmost, totake only small quantities thereof, and to discard the main quantity thereof out of the crude gases before they are liquefied, which is done in v the easiest and most efficient way by the process according to which the dephlegmation or separation is stagesof compression, using, if desired, watercooling or other artificial cooling at the same time. Theapplication of this method has shown, however, that new losses and difliculties are connected therewith, and that the efficiency of the whole apparatus is much decreased as soon as the above-mentioned dephlegmation is carried on energetically.- Thorough investigations have shown that there qre) the following reasons for these facts: n discarding thoroughly easily volatile liquid hydrocarbons which form 25% to 30% of the weight of the heavy crude gas that has been made at low temperature,

are taken out of the gas, which naturally results in the decreasing of the quantity of the condensed products- (liquefied illumi-' nating gas) which are obtained by compression and water-cooling; it decreases,

however, not only because the weight of the discarded" easily volatile liquid hydrocarbons has to be deducted, but also for the reason that because they are no longer contained in the liquefied gas, those gaseous constituents which otherwise would have been dissolved therein escape together with the permanent gases. Thus the partial pressure of these liquefiable gases, contained in the permanent gases which are gathered above the liquid gases, increases correspondingly to the increase in quantity of those liquefiable gases and the whole quantity of the non-liquefied gases obtained as a byproductincreases in the same proportion. Therefore, in this case, in order to recover by absorption the liquefiable constituents out of the permanent gases, firstly, acorrespondingly larger quantity of absorbing liquid has to be used-and, secondly, a larger J39 quantity of gas becomes free upon the release of the pressure and has to be compressed again. Besides the fact that, therefore, with the abovedescribed method of erable quantity of power, another fact has to be considered, namely, that the gases released from the liquid, upon the release of the pressure, are carrying with them considerable quantities of vapors of the absorbing liquid; for the easily volatile hydrocarbons, for example, those which have been discarded from the crude gas itself by cooling or during compression, are used for, and are especially adapted for use as, an absorbing fluid. These vapors carried by the released gases can, it is true, without complicating the process, be discarded, during subsequent compression, at the same time as easily volatile hydrocarbons contained in the crude gas are discarded. As stated above, the more energetic dephlegmation of the crude gases results, however, in a greater quantity of absorbed gases circulating in the process, and at the same time the quantity of vapors of the absorb ing liquid, which have to be discarded again during the compression, increases, and the addition of these to the crude gases has an effect directly contrary to the desired purpose of discarding easily volatile hydrocarbons. The more energetic application of the dephlegmation considerably decreases, therefore, the efficiency of the manufacturing process, firstly, on account of the fact that, in the process heretofore in use, larger quantities of absorbing liquid and the gases released therefrom have to circulate as ballast through the apparatus between considerably different pressures, and, secondly, because the vapors of the absorbing liquid which are carried by the released gases have considerably increased in quantity and have to be discarded also.

The present invention concerns an apparatus for the production ofliquified illuminating gas, which does away with the difliculties mentioned above by using artificial cooling, instead of the absorbing process, for the recovery of the liquefiable constituents from the permanent gases. According to this process, the compressed crude gases, from which easily volatile liquid hydrocarbons havebeen separated, as by compression at a low stage of compression, are at first led through the pipe 1" into a dephlegmating vessel D (Fig. 1) in which settle those constituents of the gas, which have already become liquid by compression and water cooling at normal temperature or at the, temperature of the cooling Water, whereas the permanent gases, which are above the liquid and are carryin however, liquefi able gases in suspende form, are submitted as thoroughly as possible to strong artificial cooling, whereby the liquefiable constituents are separated out in liquid form. For this purpose the permanent gases are led, for instance, out of the vessel D through the pipe 1', into the cooler G, which it is advisable to construct according to the cotmter-cm'rent principle, as shown in the drawing, and from there they are led into the dephlegmat-ing vessel 1),, where the constituents that have become liquid by the artificial cooling separate from the constituents that have remained permanent gases. These permanent gases are then led away through the pipe 7'. whereas the condensate flows back through the pipe r which is connected with a hydraulic valve it, into the dephlegmatingvessel D. According to the partial pressure of the liquefiable and permanent gases in the original mixture led into the dephlegmating vessel D through the pipe 1* and according to the temperature of condensation that has been obtained by the cooler G and according to the pressure existing, the condensate con tains, dissolved therein, a larger or smaller quantity of permanent gases, which, however, escape from the liquid in gaseous form when this liquid comes in contact with the liquid-of a considerably higher temperature, for example, normal temperature, already contained in vessel D. This results in a gradual cooling down of the' liquid gas which is contained in D as the condensation process goes on; and this increases its quality to dissolve permanent gases, and it has been found that when this cooled gas was filled directly from I) through pipe 7', into the shipping vessels (where it assumes normal temperature), it loses the homogeneity of its liquid state and passes partly again into gaseous form, preventing, thereby, the possibility of filling the bottles with the necessary weight. This can be avoided, however, by adding, before the filling, so much heat to the liquid gas that is gathered in the lower part of vessel D that the permanent gases dissolved therein are driven out and that the liquid gas itself is warmed to, or kept at, approximately normal temperature or a temperature a little above that. This additional heat can be taken from any source of heat; it can be acquired, for example, by leading the gas to be liquefied in its over-heated condition, as it is obtained, for instance, by compression without simultaneous water copling, through a heating coil H (Fig. 2) which is placed in the lower part of D. As the compressed gas has the o portunity to give off in H the heat resulting from its compression, it liquefies, in part at least, and then is introduced into D itself for further treatment as described above.

/ It is advisable to increase the efficiency of the separating apparatus D by constructing 5 which are provided with or leave alternatin openings 0 along the length of the vessel and which prevent the circulating of the liquid and the gases inside of the apparatus but allow the condensate to move in layers of corresponding specific gravity in the direction from the top to the bottom only, whereas the gases are allowed to rise from the bottom to the top. If, in this way, the lighter layers of the liquid and gas are gathered above the heavier layers, it furthermore seems to be advantageousto introduce the mixture ofconstituents which have already been liquefied and of constituents which are still gaseous, not directly from the heating coil H into the column D but to let it pass first through one or several separating vessels, 1),, D in each of which the liquid is separated from the gaseous constituents. In order not to interfere with the rectification process that is going on in the column D, the.

liquid coming out of D for instance, is introduced into column D through pipe 1", at

a point or place of the column where the gas mixture in the column itself has approxigoimately the same temperature and the same composition as the liquid introduced from 1),. i The gases gathered above the liquid in D are led from there through pipe 1",, into a cooler l/V, where they are cooled off to the temperature of cooling water (about 10 (1). Consequently, another part of the gas is here separated out and gathers in D below the gases which have not been liquefied and come out of W at the same time. Naturally, the composition of this liquid'is different from that of the liquidin D which has been obtained at a higher temperature out of the still heavier gases. The condensate obtained out of D is the lighter one and contains a higher percentage of permanent gases in solution. Therefore it is introduced into the column through pipe r, at a place higher up than that obtained out of D The gases that are not separated out as liquids in D are led from there througha pipe 11., through the counter-current cooler G, and

may there be submitted to a further cooling process, by leading the cooling agent, which has already been used at a lower temperature in the apparatus G through pipe 1, into G,, where it is again used as a cooling agent. The gases which have been cooled in G, considerably lower than the temperature of the cooling water and which have been partly liquefied are led from there through pipe r into the column D at a place which is higher up again than that which was chosen for the introduption of the condensate coming from D 1 For the operation of the process just described the cooling a cut, chosen for the cooling of the gases w ich are led throu h the counter-current apparatuses G and 1 in order to cool them down to their tern-L perature of condensation, is important. To

secure the low temperatures employed, a

.is by far too small to obtain from them a sufiicient cooling to the required temperatures and to obtain a sufficient condensation of the liquefiable constituents which are contained in the gases to be cooled. These gases will cool down the gas only to atemperature at which some only of the liquefiable constituents contained in the gas at this point are recovered and at which the permanent gases comingout of D still contain a considerable percentage of liquefiable constituents, which, consequently, are not recovered as liquids. The operation of the process has given satisfactory results, however, if one part of the gas already liquefied is used as a cooling agent. This, for instance, may be taken out 'of the lower part of column D throughpipe r, and be led through pipe 1' to the regulating valve V (Fig. 4) and to the counter-current apparatus G, where itescapes under the suction pressure of the compressor K. With the comparatively great cooling effect thus obtained, it is possible to reach very low temperatures, down to 0., if the liquefied gas, before being. treated in the column D, was substantially freed from easily volatile or carbureting liquid hydrocarbons. A still greater decrease of temperature can be obtained if the liquefied gas, which consists mainly of ethylene, is taken, as by pipe r from a higher place of the apparatus D, even where it still contains, in solution, a considerable quantityof methane and a small percentage of hydrogen. However, if the column D has been constructed in a proper way, the employment of such very low temperatures is not necessary to the practical efficiency of the separation. If the liquefied gas that has been obtained out of the process itself is used as a cooling agent, it gives the further advantage that it is not necessary to allow it to .expand under the pressure of the suction piper of the first stage of compression but that it may be allowed to expand underthe pressure of the suction pipe 11 0r 1' of the second or third stage of com pression, whereby the desired cooling effect is obtained and the expenditure of less power is required to compress again the expanded gas than would be required it the liquid gas were permitted to expand at the pressure of the suction pipe of the first stage of compression. In this case, the gas that has vaporized or expanded and is still under pressure is sucked into the compressor again through, for instance, pipe 73 and is again compressedf Whereas, with the method first described, where the cooling agent vaporized or expanded under the pressure of the suction pipe 1' of the first stage of compression andwas sucked into the compressor again by said pipe 03,, the

efliciency of the compressor K was decreased,

because, in such case, the first cylinder is of the compressor K can receive and compress a smaller quantity of the crude gases on account of the presence of said expanded gases that have to be again compressed by it; but the efficiency is not decreased with the method last described and it requires less power to compress again the gas that has been used as a cooling agent.

As will be understood by those skilled,

in the art to which this invention appertains, variations may be made in details without departing from the main features of the invention.

Obviously the liquefied gas, made in accordance with this invention, can, in the usual manner, as by an admixture of air, be employed for the production of a nonluminous flame of great heating power adapted to heat to incandescence Welsbach mantles or other suitable objects and for numerous other purposes.

Among many other advantages that can be secured by the present invention are the advantages that a much greater volume of liquefied gas made according to this invention than of that heretofore made can be filled into containers for shipment or use and at a lower pressure; that the permanent gases and easily volatile hydrocarbons can be more thoroughly separated out with satisfactory results in the product; that liquefiable gases, which heretofore were carried away with permanent gases, can nearly all be recovered and made part of the liquefied gas; and that the liquefied gas can be made of a more uniform composition.

What I claim is 1. In apparatus for liquefying gaseous mixtures, the combination of a separatlng vessel, a cooler, a second separating vessel, means for the passage of gas from the first separating vessel to the cooler and into the second separating vessel, and means for leading liquefied gas from the second separating vessel into the first separating vessel, substantially as described.

2. In apparatus for llquefylng gaseous "mixtures, the combination of aseparati'ng vessel, means, passing through the separating vessel, for leading crude gases into the separating vessel, a cooler, a second separating vessel, means for the passage of gas from the first separating vessel to the cooler and into the second se arating vessel, and

means for leading liquefied gas from the second separating vessel into the first separating vessel, substantially as described.

3. In apparatus for liquefying gaseous mixtures, the combination of a separating vessel, means, provided with a coil situated in said separating vessel, for leading crude gases into the separating vessel, a cooler, a second separating vessel, means for the passage of gas from the first separating vessel to the cooler and into the second separating vessel, and means for leading liquefied gas from the second separating vessel into the first separating vessel, substantially as described.

4. In apparatus for liquei'ying gaseous mixtures,the combination of a separating vessel (D means for leading crude gases to the separating vessel, a second separating vessel (D), means for leading gas and means for leading liquefied gas from the first to the second separating vessel, a cooler (G), a third separating vessel (D means for leading gas from the second separating vessel to the cooler and into the third separating vessel, and means for leading liquefied gas from the third separating vessel into the second separating vessel, substantially as described.

5. In apparatus for liquefying gaseous mixtures, the combination of a separating -for leading liquefied gas from the first to the second separating vessel, a cooler (G),

a third'separating vessel (D means for leading gas from the second separating vessel to the cooler and into the third Separat ing vessel, and means for leading liquefied gas from the third separating vessel into the second separating vessel, substantially as described. Y

6. In ap aratus for liquef ing gaseous mixtures, t e combination 0 a series of separating vessels (such as D D means for leading crude gases thereto, an additional separating vessel (D), means for leading liquefied gases from the separating vessels of the series to the additional separating vessel, means for leading gases from each separating vessel of the series to another separating vessel, a cooler (G), and a further separating vessel (D means for leading. gas from the additional separating vessel (D) to the cooler and into the further separating vessel (D and means for leadcooling gases passing through the series of separating vessels, an additional separating vessel (D), means for leading liquefied gases from the separating vessels of the'series to the additional separating vessel, means for leading gases from each separating vessel of the series to another separating vessel, a cooler (G), and a further separating vessel (D means for leading gas from the additional separating vessel (D) to the cooler and into the further separating vessel (D and means for leading liquefied gas from the further separating vessel into the additional separating vessel, substantially as described.

8. In apparatus for liquefying gaseous.

mixtures, the combination of a series of separating vessels (such as D D means for leading crude gases thereto, an additional separating vessel (D), means for leading liquefied gases from the separating vessels of the series to the additional separating vessel at diiferent elevations, means for leading gases from each separating vessel of the series to another separating vessel a cooler (G) and a further separating vessel (D means for leading gas from the additional separating vessel (D) to the cooler and into the further separating vessel (D and means for leading liquefied gas from the further separating vessel into the additional separating vessel, substantially as described.

9. In apparatus for liquefying gaseousmixtures, the combination of a series of separating vessels (such as D D means for leading crude gases thereto, means for cooling gases passing through the series of separating vessels, an additional separating vessel (D), means for leading liquefied gases from the separating vesselsfof the series to the additional separating vessel at different elevations, means for leading gases from each separating vessel'of the series to another separating vessel, a cooler (G) and a further separating vessel (D means for leading gas from the additional separating vessel (D) to the cooler and into the further separating vessel (D and means for leading liquefied gas from thefurther separating vessel into the additional separating vessel, substantially as described.

10. In apparatus for liquefying gaseous mixtures, the combination of a series of separating vessels (such as D D means for leading crudegases thereto, an additional separating vessel (D) constructed as a rectification column, means for leading liquefied gases from the separating vesselsof the series to the additional separating vessel at separating vessel into the additional separating vessel, substantially as described.

11. In apparatus for liquefying gaseous mixtures, the combination of a series of separating vessels (such as D D means for, leading crude gases there-to, means for cooling gases passing through the series of separating vessels, an additional separating vessel (D) constructed as a rectification column, means for leading liquefied gases from the separating vessels of the series to the additional separating vessel at difierent elevations, means for leading gases from each separating vessel of the series to another separating vessel, a-cooler (G) and a further separating vessel (D means for leading gas from the additional separating vessel (D) to the cooler and into the further separating vessel (D and means for leading liquefied gas from the further separating vessel into the additional separating vessel, substantially as described.

12. In apparatus for liquefying gaseous mixtures, the combination of a separating vessel, a cooler, a second separating vessel, means for the passage bf gas from the first separating vessel to the cooler and into the second separating vessel, means for leading liquefied gas from the second separating vessel into the first separating vessel, and means for leading a constituent of the compressed, crude gases from one of the separating vessels into the cooler, substantially as described.

.13. In apparatus for liquefying gaseous mixtures, the combination of a separating. vessel, a cooler, a second separating vessel, means for the passage of gas from the-first separating vessel to the cooler and into the second separating vessel, means for leading liquefied gas from the second separating vessel into the first separating vessel, and means for leading liquefied gas from one of the separating vessels into the cooler, substantially as described.

14. In apparatus for liquefying gaseous mixtures, the combination of a separating vessel, a cooler, a second separating vessel,

15. In apparatus for liquefying gaseous mixtures, the combination of a separatin vessel, a cooler, a second separating vesse, means for the passage of gas from the first separating vessel to the cooler and into the second separating vessel, means for leading liquefied gas from the second separating vessel into the first separating vessel, and means for leading liquefied gas from an upper part ,of the first separating vessel into the cooler,

substantially as described.

16. In apparatus for liquefying gaseous mixtures, the combination of a separatin vessel, a cooler, at second separating vesse, means for the passage of gas from the first separating vessel to the cooler and into the second separating vessel, means for leading liquefied gas from the second separating vessel into the first separating vessel, means for leading a constituent of the compressed crude gases from one of the separating vessels into the cooler, and a valve for regulating the flow of the constituent of the crude gases into the cooler, substantially as described.

17. In apparatus for liquefying gaseous mixtures, the combination of a com ressor, a separating vessel, a cooler, a secon separating vessel, means for leading compressed, crude gasesfrom the compressor to the first separating vessel, means for leading as from the first separating vessel to the coo er and into the second separating vessel, means for leading liquefied gas from the second separating vessel into the first separating vessel, means for leading a constituent of the compressed, crude gases from one of the septhe passage of gas connecting the cooler with the compressor, substantially as described.

18. In apparatus for liquefying gaseous mixtures, the combination of a compressor provided with several cylinders adapted to compress crude gases at different stages of compression, a separatin vessel, a cooler, a second separating vessel, means for leading compressed crude gases from the compressor t0 the first separating vessel, means for leading gas from the first separating vessel to the cooler and into the second se arating vessel, means for leading lique ed gas from the second separating vessel into the first separatin vessel, means for leading a constituent of tie compressed, cr ude gases from one of the separating vessels into the cooler and means for the passage of gas connecting the cooler to a cylinder of the compressor adapted to compress the crude gases at one of the higher stages of compression, substantially as describe HERMANN BLAU.

Witnesses:

LINA DISGHL, RICHARD LEMP.

arating vessels into the cooler and means for