DE1198333B - Device for the extraction of elemental sulfur - Google Patents

Description

FEDERAL REPUBLIC OF GERMANY

GERMAN

PATENT OFFICE

EDITORIAL

Int. α .:

COIb

German class: 12 i - 17/04

Number:
File number:
Registration date:
Display day:

1198 333
P 20438IV a / 12 i April 1, 1958 August 12, 1965

The invention relates to a device of compact design for the extraction of elementary Sulfur in particular from gases containing hydrogen sulfide.

From many gases, such as B. natural gas, petroleum,. Coke oven gas and the like must contain the hydrogen sulfide present must be removed, as this is not only highly corrosive, but also as a strong poison is known. It is economically important to process it for the extraction of elemental sulfur, for which there is a great industrial need.

The extraction of elemental sulfur from so-called "acid" gas streams, such as z. B, natural gases, reacting the entire feed with air or other oxygen-rich Reactants, after cooling the hot gas mixture, some sulfur in one with one pressure-tight jacket surrounded combustion boiler is obtained. From this leaving and at

Device for the extraction of elemental sulfur

Applicant:

Pan American Petroleum Corporation, Tulsa,

OkIa. (V. St. A.)

Representative:

Dr.-Ing. H. Ruschke, patent attorney, Berlin 33, Auguste-Viktoria-Str. 65

Named as inventor:

Maurice Webb, Tulsa, OkIa. (V. St. A.)

th gases after adjusting to the stated temperature range, passing through a second reaction zone and a second washer more free Sulfur won.

After dividing a feed stream, one third of this is sulfur dioxide burned and reunited with the remaining two thirds to form a mixture that is approximately equi-

or gases containing these in a closed, insulated against heat loss chamber of a fire box boiler, at the upper end of which a reaction mixture held at about 205 to 230 ° C and next to it a feed water are arranged after being blown into a with a warmer, through which the combustion Catalyst-filled reaction _{zone draw an H 2} S circulating gas from top to bottom. When cooled, it converts into elemental sulfur up to 75%. After letting down to about ISO ⁰ C, part of the sulfur is eliminated in liquid form by letting the gaseous products spread and the remaining part is converted into a preheater or condenser one filled with Raschig rings

Separator out, with still remaining hydrogen sulfide and remainder in the gases generated Sulfur dioxide can be converted into sulfur in further dust chambers.

In the system for the so-called "Claus process", the condensation section is separated operated from each zone of the boiler. There the gases pass through a large one and one surrounding it

is equivalent to that generated when the entire pipe is smaller and gas is passed through the boiler and processed before it leaves the system. mixed by a special pipe.
Two converters were used here, and the on- With all these known constructions

processing of the current through the system and the condensation and heating or combustion separation of elemental sulfur is not essential in the section together with a heat the same as in the manufacture of an exchange device arranged in a single boiler, batch mixture by introducing the starting material In contrast, the subject of the invention is a

in the furnace and its burning to sulfur dioxide. Device of compact design for the production of elemental sulfur by combustion of the same parts of the apparatus, namely a boiler, two hydrogen sulfide with air and O ₂ -containing gases, converters, two condensers and for each of 45 conversion of the gas into at least one of these a separating device for gas and liquid catalytic stage and separation of the sulfur formed in one phase, two reheaters or series burners, and condensation section for each catalytic stage, a lot of space required, formed by condensation, the

According to another known method wins is characterized in that a combustion man. B. sulfur through combustion of sulfur chamber (84), a device (108) for cooling hydrogen or gases carrying these by means of combustion gases and two condensation sections downstream of the catalytic combustion with a free flame with the aid of oxygen stages

509 630/333

(120,122) in a single steam generator- Fig. 12 is a cross-sectional view of

supply system provided boiler (4) are housed. F i g. 11 along the line DD;

Additional reheaters are not required here or FIG. 13 is a partial end view, partly in section,

Series burner for regulating the temperature of the separator and collecting treatment gas according to the invention to the converters, also with 5 container combination;

Drain lines provided with steam jackets because all of FIG. 14 is a sectional plan view along the lines of FIG

Install the pipelines yourself, as well as the line E-ii from Fig. 11, and

Use of special separators for gas F i g. 15 is one such view of the

shaped and liquid ,. Phases for each individual separating and collecting container for liquid sulfur Condenser by the design of a new Sepa- io with an exact reproduction of the pipeline system for rator and collection container, as well as all equipment handling of the gaseous and liquid productions for preparing boiler feed water. The tes that flows to the separator and for that from it the latter can be achieved z. B. by using the escaping gas in.

Like reference numerals refer to like

Boiler as described in the Girbotol desulphurisation 15 parts in all figures in connection with the systems for H ₂ S-haIg gases ("acid" gases). Generally speaking, it is used to make use of the generated steam. management of the method according to the invention specifically

The device for the extraction of elemental one with a single steam generation system from sulfur According to the invention, the combination of armed boiler 4, in which essentially the lower an elongated enclosed metal kettle so half a main heating section and steam pipes with a combustion chamber, a device · -. Sulfur water becomes in the heating section Blowing in air and the gas to be processed, creating temperatures up to anin this chamber and near its opposite one approaching 1200 to 1400 ° C and below that sufficient-end with their interior in connection with the air supply that burned in the final mixture of Pipeline on the-outside of it and back to 25 hydrogen sulfide to sulfur dioxide a Molverihrem Inlet ends run. ratio of about 2: 1 is created. One at each end

Furthermore, the elongated housing of the boiler 4 has a gas-tight metal plate or plate within a part for processing ele--sheet divides the upper and lower sections of the Liquids containing mentary sulfur and build-up only on its gas side, d. H. the steam vapors at least one liquid-tight pipe in the upper skins stand with the same shared space each with its own inlet and water in contact with the steam pipes in its Outlet, a pipe touches the lower half of the partitioned off rooms. The gas side in the upper one to a common portion of the housing and half is at each end of the boiler 4 preferably a device for drawing off the liquid sulfur from a gas-tight metal plate or intermediate sulfur product from this. 35 wall divided in half. This creates separate

In the figures, a number of execution inlet areas or compartments are created for the shapes explained. Gas from each of the two converters. Hot gas

Fig. 1 is an elevational view of prior reactants being dislodged from the kettle Side of an example sulfur cut removed, some generated sulfur on it in System for explaining a special 40 section of the liquid separator and sambuilding the pipe plant and equipment; and the remainder of the reac-

Fig. 2 is a side elevational view of the participant as will be described later Structure according to Fig. 1; fed into the first converter. After implementation in

Fig.3 is a side elevational view of the first converter converting the generated gas to the as new part of the Kes equipped with a single steam generation system 45 condensation section Boiler 4; let 4 go for processing. The resulting

Fig. 4 is an end view of kettle 4 after condensate passes along with the non-condensate fig. 3, which then goes into more detail about the position of the two gases, first in a separator. To Main sections of the combustion system (heating system), separation of sulfur in a section of the d. H. the boiler section and the condensation drain 50 liquid separator and collection tank leads reproduces cuts; the uncondensed reactants to

Fig. 5 is a cross-sectional view of the second converter vessel 4, and the general condenser Fig. 3; sation process, the sulfur separation, etc. are

Fig. 6 is a more detailed illustration of the repeated at the condensation stage, this time Heating section in F i g. 5; 55 is going on in a part of the boiler that is from the

F i g. 7 is a fragmentary, longitudinal, end elevation view, majorly different and separated, in which the generated neutrally condensed in the section of boiler 4 with no front side sulfur from the first converter cover; became. That during simultaneous oxidation

Fig. 8 is a front end view of about one third of the hydrogen sulfide to the boiler tube wall of Fig. 3 taken along the 60% sulfur dioxide and condensation obtained from line AA; Gas generated from the converter is how steam

Fig. 9 is a rear view of the boiler tube generally indicated, withdrawn from the boiler 4 wall of Fig. 3 along the line BB; and, if desired, can be added to a system part in

F i g. 10 is a cross-sectional view of FIG. 6 the steam is used as a heating medium, or along the line CC; 65 be conducted to a suitable elevated condenser

F i g. Fig. 11 is a view in elevation, partly in section, showing that the condensate formed is lost novel separator and collection container for the water or liquid side of the boiler 4 by gradient liquid sulfur; is returned. In this way the boiler

sation section of the boiler 4. In its upper part the sulfur vapors obtained are condensed into liquid sulfur, and this comes together with non-condensed gases through outlet 66 (Fig. 3), directly opposite outlet 65, and line 48 to receiver 24 where said gases are from the liquid sulfur product separated and discharged through a chimney (not shown here).

The steam generated in the upper as well as lower sections of the boiler 4 is through a Steam outlet nozzle 49 and line 50 discharged at a pressure of about 22.7 kg absolute. This one Steam can be used for heating during the procedure

indicated, lead and the resulting condensate back into the boiler 4 via line 53 and inlet 80 lead back.

The overall system structure, as shown in FIGS. 1 and 2 with the individual apparatus sizes is shown, stands about 6 m high and occupies an area of about 30.60 m ² . The boiler itself can be 4.75 to 6 m long with a diameter of 1.52 to 2.43 m

self feed water continuously to the plant part
Delivered without further treatment.

1 and 2 are front and side elevational views, respectively, of a preferred arrangement
reproduced by pipe system and equipment as an embodiment of the invention. Air gets through
Line 2 supplied and with the through line 6 in
the combustion system in the boiler 4 mixed hydrogen sulfide-containing ("acid") gases.
This boiler rests on an I-beam 8 and this io
again on a cement foundation 10 used in a concrete substructure 12.
the supporting structure intended for holding the boiler 14 includes the vertical I-beam 16, which is placed on the

15 supported by the concrete substructure 12 or "can be used for other purposes. So you can use it on the foundation 18. Boiler 14 has two gas-tight _{compartments, each for} a suitable condensation system, for example, as 51 provided with a catalyst bed Support structure more stable and
transfers the weight of the boiler 14 to the support pillar 16. The boiler 4 is at an angle of 20
inclined about 5 °, so that the elemental sulfur condensed in it or that from oxidation
from a third of the hydrogen sulfide to sulfur dioxide with the process streams from the rear part of the boiler 4, removed through line 22 and 25 _sem> the separator and collecting tank at a to the partially submerged gas-liquid Sepa diameter of 1.82 to 2.43 m a length of rator and collecting container 24 is sent, which have in 7 ^ 2 to 9.14 m. The total length of the boiler, a cement base 25 is inserted. Usually providing the service of two reactors, the container 24 can be at a temperature of about a diameter in the range of 1.82 to 120 to about 150 ° C by the sulfur produced 30 to about 3.65 to 2.42 m 4.57 m, the power and through the hot gas streams from the process capability of a system of such dimensions or held so that the resulting liquid sulfur in size in the range of about 9072 kg to about pumpable and free-flowing consistency is 22,680 kg Sulfur per day will be. The exposed portion of the container 24 may be shown in FIG. 3 and 4 are single-sided or end faces that are covered with insulation, which in turn, 35 side views of the boiler4. Thus, in FIG. 3, a metal jacket can be protected, if desired, by means of an entry access 52 (not shown here) to the steam section of the boiler 4. Provided together. The extension pipe 54 serves as a pipe connection with the sulfur product, which passes through the line 22 for the boiler pressure relief valve Ends on the base of the boiler 4 for occasional stages in the boiler 4 remains. This gas-like cleaning. An outlet 60, which comes from a point from the first separator section in the vessel close to the end face of the lower boiler half front 24 through the line 26 and is jumps out with hot, carries hot bypass gases mixed from the Behei bypass gases coming from boiler 4 in a tongue tube for previously explained purposes away. An off three-way valve 28 come. The bypass gas is 45 let 62 on the opposite side of boiler 4 proportionally leads the reactants in line 26 also hot bypass gases from the heating tube, adjusted so that the temperature of the resultant, as explained, away. An inlet 82 receives the mixture in line 30, which then in the product gas from the second catalyst chamber, first catalyst chamber in the boiler 14 passes, in the _un d it leads to the second condensation section desired initial temperature of approximately 230 ° C 50 of the furnace. After condensation has occurred, it lies. The generated gas from the first catalyst chamber in the boiler 14 is withdrawn through line 38 and to the first condensation section of the
Boiler 4 sent through inlet 64. The condensed sulfur produced is drawn off together with non-55 "Fig. 4 shows the front end of the furnace, the main converted gas through the outlet 65 and line consists of flat plates 68 and 70. These are drawn off and the second separating section
supplied in the container 24. Uncondensed reactants exit this separation section through line 44 and mix with 60. You can also remove the three-way valve 46 from the boiler 4 by means of a carrier 72 on a vertical steel hot bypass valve and the three-way valve 46 on a horizontal component 74. The resulting screwed. Handhole flaps 76 and 78 are used for the mixture, the feed gas to the second for access to the separate condensation catalytic converter chamber and is there by cutting the furnace. An inlet 80 takes condensation 32 transferred. Hot generated gas (product water and feed it to the steam section of the gas) is released from the bottom of the second catalyst boiler 4. Inlets 64 and 82 take the gas extracted from the first and second catalyst chambers in the boiler 14 through line 40 and enter the second condensation chamber through inlet 82 in accordance with the general explanation above.

the mixture of the non-condensed gases plus liquid sulfur product Condensation section withdrawn through outlet 66.

can be attached to the boiler 4 by screwing it to a flange-mounted frame, the one with the shell part of the boiler

7 8

th process, as described in detail also on the lower side of the steel plate 114,

is written on. which forms the bottom of the chamber UO, attached and

5 is a cross-sectional view of the newly protecting the latter against the high temperatures prevailing in the lower-like, inventive construction of the kes chamber 110 , sel 4, which has a cylindrical casing 83 at its rear, lower end the furnace has the combustion section (heating tube) 84 closed by means of a steel wall plate 116 which contains * in the "acid" gas and air through which is provided with a handhole flap 118 so that inlets 6 and 6 respectively. 2 stream. As seen from the front, there is access to the inner sections of the structure which surrounds part of the heating section 84 and which is in communication with chamber 110. Refractory material 88. It has a rear metal. The entire interior of the boiler 4, which is covered with the hot metal cover plate 86, which comes into contact with the hot combustion acid gases, is preferably made by means of a castable fire with a suitable protective jacket such as B, solid material 89 is protected. Combustion plays with sodium silicate, coated. This area seen in the heating section (combustion chamber) 84 protrudes from the interior of the chambers 100,106 and, The hot process oars ig 110 generated in this, as well as the two, with the condensation strokes then through outlets near its end, sections 120 and 122 ( Fig. 7) in connection of which one (102) is shown here. Then standing chambers. One of the two named, these gases enter pipes 108 , in which the end chamber is shown as 121 and valid cooling in the boiler section comes to an end with the condensation section 120 . Parts of the combustion chamber 84, the aö bond,

not water-cooled on the steam side of the boiler 4 Fig. 7 is a longitudinal partial view of the, as well as other parts of it, such as a Kam boiler 4, with the cover plate removed. Here ffler 106, which are exposed to temperatures above 425 ° C, can clearly be seen the construction of the gas-tight sections are made of castable refractory material sections at the front end of the boiler 4. The gas-protected 88 and 125 return pipes 103 and 25 are tight sections at its rear end in 104 (FIGS. 6 and 8) should be dimensioned in such a way that an identical design is formed. Here, the hot gases emerging from them are shown on a vertical plate 126 in such a way that they have a temperature of about 535 to 1100 ° C. from the raw *. ren 94 to the front edge of the horizontal divider - If they are too hot, then they cannot protrude into a back plate 124 , whereby they are passed on to a gas-tight, conventional three-way valve 30 blocking between the condensation sections 120 (Fig. 1 at 28 and 46) . If they are too cold, one and 122 is enabled and the chambers 121 and 123 are discharged in excess in order to form the desired connection with the sections 120 and 122 in kunggas to the catalyst chambers.

Maintain temperatures. The at the pipe Fi g. Fig. 8 is a front view of the tubes 94 shown in Fig. 3, plates 96 and 98 attached to take from boiler 4 along line AA. With the catalyst chambers receiving hot generated gases, cover plates 68 and 70 removed. The upper and (Fig. 4) through the inlets 64 and 82 in the lower end face sections are only boiler 4 enter on the gas side and divided into separately delimited cones with the help of the horizontal steel plate 124 , condensation sections 120 and 122 are passed and the upper Half is still in the condensate (Figs. 7 and 8). The sulfur vapors sweep together sections or chambers 120 and 122 by means of men with non-converted gases through pipes 94, where a vertical, gas-tight steel plate 126 divides the sulfur converted into a liquid product. The plate 124 serves to prevent streaking. Since the boiler 4 is about Chen inclined at an angle of gas between the tube groups 94 and 5 degrees from the back to the front, he gives 108. The relative position of the Rücklaufkrümmerrohre rise to flow of the condensed sulfur 4S 103 and 104 to the heating section 84 and to the rocks in the pipes 94 as well as the in-the pipes pipes 108 is also shown.
108 to the rear end of the boiler 4 into the chambers; FIG. 9 is a view from the rear end part in 100 or UO; there it is withdrawn along with the non-section of Fig. 3 along the line 5-5 and shows converted gases generated through outlet 92 the similarity in construction of the gas side and lines 42 and 48 (Fig. 2). 5 ° at the back of the kettle to the one in its

The relationship of the return creeper tubes in FIG. 8 front end shown. The lower part

103 and 104 to the heating pipe 84 is in Fig. 6 more precisely of the boiler 4, from which the heat exchange pipes 108

shown in detail, in which one of these tubes stops, is against the condensation sections 120 and

104, it is shown being moved from a point close to 122 by means of a castable refractory material

End of heating section 84 starts up and back to 55 112 isolates the upper and lower rear parts

goes to tube plate 96. The pipes 103 and 104 of the boiler 4 are similarly connected to the gas

hen in connection with the zone 106, which in turn rarely only by a horizontal plate 114 and its

to the tubes 108 and to the three-way valve through the upper half is still by means of a vertical

let 60 and 62 (Figs. 1 and 4) lead. Plate 127 divided to cover the posterior parts of the condensate

A fireproof Schamottemateriai 105 protects the 60 sation sections 120 and 122 to form a similar end plate 68 against hot combustion gases of the type at the front of the boiler (FIGS. 7 and 8). Zone 106. In the tubes 108 (heat exchange- Fig. 10 is a cross-sectional view of Fig. 6 tubes) additional liquid sulfur can be formed along the line CC and gives further details and flows together with not around the relative position of the return manifold tubes 103 released gases, which may be returned from boiler 4 65 and 104 to the heating section 84 ,
flow out through outlet 92. A potting Fig. 11 is an elevation, partly in section, of a neubarable refractory material 112 attached by means of tackle-like container construction from a combination of welded anchors 113 , gas-liquid separator and collecting container

the end cover plates 128 and 130, which are welded to the cylindrical shell or to its main part 132 , which have an entry access 134 on the upper part side. An inlet 136 communicates with the compartment 138 , which is formed by steel prali plates 140 . 142 and 175 (Fig. 12) are welded to the end cap 128 and to the top of the cylindrical kettle. The plate 140 is made stable by means of U-beam members 144. Generated gases enter space 138 along with the liquid sulfur product through inlet 136 where the liquid sulfur flows down through a U-shaped plug tube 146 . Within the entire vessel, the temperature is generally maintained in the range of about 120 to about 150 ° C by the gases from the process, allowing free flow of liquid sulfur down through the closure tube 146 and from its opposite end into the collection zone 148 of the Container is secured, which actually serves as a third separation section. The discharge end of tube 146 is held in place by a spacer 150 attached to the discharge end and at a point directly opposite the end on the inlet side of said tube. Uncondensed gases are withdrawn from chamber (compartment) 138 through outlet 152 and returned to the reactor for further conversion of hydrogen sulfide. Exactly the same separator space 154 (not shown in FIG. 11, but explained in relation to FIG. 12) is located opposite the chamber 138 and has inlets and outlets (not shown) which are similar to the passages 136 and 152. After passage of participating in the reaction gases through the second catalyst chamber, the resulting gas product enters, together with liquid sulfur through the opening 156 in the Hauptsammeizone 148. The opposite end of the container is equipped with a pump dip tube 158, suspended from a collar 160 at the upper part of the collecting container and extends to a height of generally 50.80 to 101.60 mm above the bottom of the container. Directly under the bottom of the pump immersion pipe is a bowl-shaped flow collecting bowl 162. All gases not condensed in this process stage are drawn off from the container through the outlet 164 and led to a suitable shaft (not shown here). By using a vessel of the specified type, one can avoid steam jacketed piping and expensive separator and washing equipment used in conventionally built plants.

F i g. 12 is a view in elevation and section of the boiler of FIG. 11, taken along line DD, illustrating in greater detail the construction of the separator spaces 138 and 154 and the relationship of said compartments to the U-bend tubes 146 and 166 . between these there is a riser 170, and is used for withdrawing the condensate from Dampfsammeirohr 172. a U-bracket 144 is spot welded to the sides of the cylindrical shell 132 and the base plate 140 serves as a reinforcing member for the latter. The intermediate wall 175 extends from the plate 142 to the closure cover 128 and forms gas-tight compartments 138 and 154 with the inlets and outlets 136

ίο or 155.

F i g. 13 is a partial longitudinal view, partly in section, of a combination of the separator and collection container 24 and shows how the upright plate 175 is attached to the horizontal plate 140 to form the separation chamber 138 and 154 . Here you can see in particular how a gas-tight seal between the end plate 128, from which parts have been omitted, and the front edges of the plates 140 and 175 can be effected.

Fig. 14 is a plan view and section of Fig. 11 along the line EE and illustrates in detail the steam heating coil at the bottom of the sump with which one can maintain the appropriate temperature during the time in which the system is not in operation and gases from Do not enter the process into the heat supply container. In this system, a collecting pipe 176, which is provided with an inlet conduit 178 attached to the lines 180 and 182, which in turn distribute their vapor flow in the lines 184 and 186, respectively, all of lines 180 ends to 186 in the manifold 172nd These lines are supported by U-rails 188 and held clear from the bottom of the container. The entire structure of the steam lines is inclined so that the included, through the tank bottom, the steam pipes and even ending in the manifold 172, the angle formed is approximately 5 to 10 ° so that the condensate in the collecting pipe flow 172 and by line 170 can be deducted.

F i g. 15 shows in plan a separator and collecting container 24 and the pipe system arrangement to and from the container 24 in combination with the boiler 4 and the reactors (FIGS. 1 and 2). At the end opposite that into which the generated gases flow, a conduit 190 leads at the outlet or suction attachment 164 to the duct 192, in which unreacted product gases are withdrawn into the atmosphere. The liquid sulfur product is removed from the container through line 194 by means of a pump 196 .

The applicability of the device according to the invention in the extraction of elementary Sulfur by partial oxidation of hydrogen sulfide in a known manner and below explained Conditions, is illustrated by the following example in relation to the previous ones Figures further explained.

Table I. Together
settlement H ₂ S containing
gas air Sulfur removed
1. Separator
chamber feed
for the first
converter First
converter
Drainage First
capacitor
Drainage Sulfur removed
2. Separator
chamber H ₂ S
COS
so _Ä 36.10 7.89
0.14
4.01 2.61
0.004
1.30 2.61
0.004
1.30

509 630/333

Table I (continued)

CO ₂ xi2ö "iiaicigcs air Sulfur removed feed First First Sulfur removed z <us ammen- H ₂ O vJab 1. Separator for the first converter capacitor 2. Separator CLOSE CH ₄ 18.35 chamber converter Drainage Drainage chamber C ₂ H ₆ 5.02 1.60 15.80 15.97 15.97 C ₃ H ₈ 0.11 28.78 33.92 33.92 ^C 4 ^H 10 0.06 N ₂ 0.06 O ₂ 0.06 S ₂ 72.55 S ₈ 19.17 60.94 60.94 60.94 S ₈ S _n 0.021 total 0.14 . 0.360 0.0029 Moles per hour 0.366 1,214 0.00963 Molecular weight 59.76 93.32 14.52 (11,815) 11.815 ms (in 1000) 14.52 118.066 116.34 114.76 11.815 Temperature ° C 35.77 28.8 Pressure (absolute) 15.33 24 32.06 30.6 30.8 28.0 32.06 kg / cm ³ 49 80 30.4 29.92 29.6 1.27 1.27 149 218 315 149 149 1.20 1.20 1.17 1.13 1.13

By starting up the system constructed according to the invention and under the conditions in the table above specified conditions were 33.75 moles or 101,620.3 kg of sulfur with a recovery of 93.5% obtain.

Table II

composition Feeding to
2. Converter 2. Converter
Drainage 2. Capacitor
Drainage Sulfur removed
by
3. Separator chamber Shaft gas H ₂ S 4.12 1.48 1.48 1.48 COS 0.024 0.001 0.001 0.001 SO ₂ 2.06 0.74 0.74 0.74 CO ₂ 18.98 19.00 19.00 19.00 H ₂ O 39.40 42.02 42.02 42.02 CH ₄ C ₂ H ₆ C ₃ H ₈ , N ₂ ¹⁰ 72.55 72.55 72.55 72.55 S ₂ ² 0.49 0.002 S ₆ 0.343 0.070 0.004 0.004 S ₈ 0.0646 0.890 0.013 0.013 S _n - - (7,420) 7.42 total 138.032 136.75 135.81 7.42 135.81 Moles per hour Molecular weight 28.8 29.1 27.6 32.06 27.6 m ³ (in 1000) 35.56 35.22 34.98 34.98 Temperature ° C 232 260 149 149 149 Pressure (absolute) 1.10 1.06 1.03 1.03 1.03 kg / cm ²

One of the most salient features of sulfur recovery plants according to the invention is their compact design and the relatively low production costs. As mentioned earlier, the conventional plants with a two-converter system ten main pieces of equipment. According to the invention on the other hand, only three separate main apparatus parts are necessary for a two-converter system. So 65 it is now possible with plants that are less per day produce than 25,401.2 kg to build or construct a sulfur recovery plant that about 25% to about 50% of the cost

Claims (6)

costs, which is required for a conventional system of the same capacity. Another important factor in creating substantial cost-effectiveness in sulfur mining plants of the type according to the invention is that all lines for the process are self-draining are, d. H. the products flow off by themselves. Up until now it was necessary to remove all flue pipes enclose with a steam jacket to avoid unwanted build-up and subsequent solidification To prevent (solidification) of the sulfur. Such pipelines are expensive to lay and naturally exposed to constipation. The use of such only z. B. inclined lines for the procedure together with an ordinary steel collecting container which is an adequate Has outer insulation and is designed to act as an end separator from liquid Sulfur from gases from the process works, serves to significantly reduce plant manufacturing costs. Even when operating a heating system that is generally used in sulfur recovery systems, water treatment systems, such as intermediate tanks, feed pumps, level regulators, etc., contribute considerably to the increase in expenditure. When using a overhead condenser or an overhead process unit, such as amine reboilers, the require heating steam that is withdrawn back to the steam section of the boiler, they can usually borrow Water purification devices are omitted to make a simple, and powerful unit to accomplish. While the inventive construction is applicable to sources of "sour" gas, where If you gain about 50802 kg to 254012 kg of sulfur per day, it can of course be used for extraction serve much higher tons of sulfur with equally good results. This also applies to Sulfur recovery plants with just a single converter. The new system is made for him The latter type is suitable in that only the upper half of the boiler is made into a single one Makes condensation section and not two sections or chambers, the said single being Condensation section has only one inlet and one outlet opening. Conversion of the gas obtained in at least one catalytic stage and separation of the sulfur formed in a condensation section for each catalytic stage, characterized in that a combustion chamber (84), a device (108) for cooling the combustion gases, a condensation section (120, 122), stored above the combustion chamber (84) are housed in a boiler provided with a single steam generation system. 2. Device according to claim 1, characterized in that in the upper half of the boiler (4) a partition (126, 127) between the condensation sections (120, 122) and pipes (94) extending therefrom, in the lower half of the boiler (4) return pipes (103, 104) to the zone (106) and at the rear end of the boiler (4) chambers (100, 110) for receiving the condensed sulfur flowing off and forwarding unreacted gases to an optionally connected gas-liquid separator and Collecting container (24) are arranged. 3. Device according to claim 1, characterized in that in the upper half of the boiler (4) in front of the condensation sections (120, 122) chambers (121, 123) are provided. 4. Device according to claim 2, characterized in that in the upper half of the downstream gas-liquid separator and collecting container (24) chambers (138, 154) and under these chambers U-shaped closure tubes (146, 166) in connection with the main collection zone (148) are arranged. 5. Device according to claim 4, characterized in that in the gas-liquid separator and collecting tank (24) a pump sump (158) and a drainage pit (162) is provided below this at the bottom. 6. Device according to claim 5, characterized in that the gas-liquid separator and sump (24) having an outlet (152) connected to the partitioned space (138) and one at the other end is provided via a draft tube (192) leading to the atmosphere outlet (164). Claims: J _n Publications considered: 1. Device for the extraction of elements 50 German Patent No. 666 572; tarem sulfur by burning sulfur gmelin, manual of inorganic chemistry, hydrogen sulphide with air or _{gases containing O 2} , 8th edition, vol. sulfur, part A, 1953, p. 251. In addition 3 sheets of drawings 509 630/333 8.65 © Bundesdruckerei Berlin