PROCESS AND APPARATUS FOR REGENERATION OF A LADEN SCRUBBING MEDIUM FROM A GAS SCRUBBING

Abstract

The invention relates to a process for regenerating a laden scrubbing medium from a gas scrubbing for purifying raw synthesis gas in which the laden scrubbing medium is at least partially freed of bound gas constituents in a regeneration stage to obtain a regenerated scrubbing medium. According to the invention it is provided that after withdrawal from the regeneration stage the regenerated scrubbing medium is supplied to an intermediate vessel and the regenerated scrubbing medium is withdrawn from the intermediate vessel and supplied to an absorption apparatus for purifying raw synthesis gas. The invention further relates to an apparatus for performing the process according to the invention comprising a regeneration apparatus in which bound gas constituents are removable from a laden scrubbing medium, wherein according to the invention it is provided that the apparatus comprises an intermediate vessel into which a regenerated scrubbing medium producible in the regeneration apparatus is transferable and in which the regenerated scrubbing medium is storable.

Claims

1. A process for regenerating a laden scrubbing medium from a gas scrubbing for purification of raw synthesis gas, the process comprising the steps of: at least partially freeing the laden scrubbing medium of bound gas constituents in a regeneration stage to obtain a regenerated scrubbing medium, wherein after withdrawal from the regeneration stage, the regenerated scrubbing medium is supplied to an intermediate vessel and the regenerated scrubbing medium is withdrawn from the intermediate vessel and supplied to an absorption apparatus for purifying raw synthesis gas.

2. The process according to claim 1, wherein the gas scrubbing is a physical gas scrubbing.

3. The process according to claim 1, wherein the scrubbing medium comprises methanol as the main constituent, preferably consists of methanol.

4. The process according to claim 1, wherein laden scrubbing medium is withdrawn from the absorption apparatus and subsequently supplied to a decompression stage to obtain laden scrubbing medium having a reduced concentration of bound gas constituents which is withdrawn from the decompression stage and supplied to the regeneration stage.

5. The process according to claim 1, wherein the regenerated scrubbing medium is cooled after withdrawal from the regeneration stage and/or after withdrawal from the intermediate vessel.

6. The process according to claim 5, wherein the cooling is carried out by indirect heat transfer to a cold, laden scrubbing medium.

7. The process according to claim 1, wherein after withdrawal from the intermediate vessel the regenerated scrubbing medium is compressed to a pressure suitable for operating the absorption apparatus.

8. The process according to claim 1, wherein an amount of regenerated scrubbing medium present in the intermediate vessel is established as a controlled variable via a fill level of regenerated scrubbing medium in the regeneration stage.

9. The process according to claim 1, wherein the supplying to the intermediate vessel is carried out continuously or periodically or in batch operation.

10. The process according to claim 1, wherein the laden scrubbing medium is regenerated by stripping, preferably is regenerated by stripping with scrubbing medium vapour, in the regeneration stage.

11. The process according to claim 1, wherein the raw synthesis gas comprises at least carbon monoxide (CO), hydrogen (H.sub.2), carbon dioxide (CO.sub.2) and hydrogen sulfide (H.sub.2S) and optionally at least one element from the group consisting of carbonyl sulfide (COS), mercaptans (RSH), hydrogen cyanide (HCN) and ammonia (NH.sub.3).

12. An apparatus for regenerating a laden scrubbing medium from a gas scrubbing for purification of raw synthesis gas comprising the following constituents in fluid connection with one another: a regeneration apparatus in which bound gas constituents are removable from a laden scrubbing medium; and an intermediate vessel into which a regenerated scrubbing medium producible in the regeneration apparatus is transferable and in which the regenerated scrubbing medium is storable.

13. The apparatus according to claim 12, wherein a pump for compressing the regenerated scrubbing medium is arranged downstream of the intermediate vessel.

14. The apparatus according to claim 12, wherein a heat exchanger for cooling the regenerated scrubbing medium is arranged upstream and/or downstream of the intermediate vessel.

15. The apparatus according to claim 12, wherein the regeneration apparatus comprises a stripping column comprising a reboiler, overhead condenser and at least one gas-permeable tray.

16. The apparatus according to claim 12, wherein the intermediate vessel has an actuated device for flow rate control arranged upstream of it.

17. The apparatus according to claim 16, wherein the regeneration apparatus comprises a control apparatus for controlling the flow rate of the actuated device via a fill level of regenerated scrubbing medium in the regeneration apparatus as a controlled variable, thus establishing a fill level of regenerated scrubbing medium in the intermediate vessel.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0067] The invention is more particularly elucidated herein below by way of an example without limiting the subject matter of the invention. Further features, advantages and possible applications of the invention will be apparent from the following description of the working example in conjunction with the drawings.

[0068] FIG. 1 shows a schematic flow diagram of a process/an apparatus 100 for regenerating a laden scrubbing medium according to the prior art,

[0069] FIG. 2 shows a schematic flow diagram of a process/an apparatus 200 for regenerating a laden scrubbing medium according to the prior art,

[0070] FIG. 3 shows a schematic flow diagram of a process/an apparatus 300 for regenerating a laden scrubbing medium according to one embodiment of the invention, and

[0071] FIG. 4 shows a schematic flow diagram of a process/an apparatus 400 for regenerating a laden scrubbing medium according to a further embodiment of the invention.

DETAILED DESCRIPTION OF THE INVENTION

[0072] FIG. 1 shows a schematic flow diagram of a process or an apparatus 100 for regenerating a laden scrubbing medium such as is known from the prior art. In the comparative example of FIG. 1 methanol is used as the scrubbing medium and regenerated using an apparatus for hot regeneration. Cold methanol laden with undesired synthesis gas constituents and withdrawn from a flash stage (not shown) arranged downstream of an absorption apparatus (not shown) was supplied via conduit 101. The cold methanol in conduit 101 is laden at least with hydrogen sulfide (H.sub.2S) and hydrogen cyanide (HCN) as components to be removed. The cold laden methanol is preheated with regenerated methanol in countercurrent in indirect heat exchanger 102 and supplied via conduit 103 to the regeneration apparatus 105.

[0073] Regeneration apparatus 105 comprises a reboiler 106 in a lower region, a chimney tray 107 in a middle region and an overhead condenser (not shown) in an upper region. The methanol vapours produced by the reboiler 106 expel the undesired components H.sub.2S and HCN from the laden methanol and the components exit the regeneration apparatus via conduit 108 together with methanol not condensed by the overhead condenser. Once methanol has been condensed out of the gas mixture, the remaining gas mixture of H.sub.2S and HCN is subsequently supplied to a Claus plant for sulfur recovery (not shown). Methanol accumulated in the lower region of the regeneration apparatus has been enriched with water and is withdrawn via conduit 109 and supplied to a distillation apparatus (not shown) for methanol/water separation.

[0074] Regenerated methanol condensed by the overhead condenser collects on the chimney tray 107. Chimney tray 107 is fitted with a fill level measuring apparatus 111 (LI=level indication). Fill level measuring apparatus 111 makes it possible to measure and check the fill level on chimney tray 107 but not to control the fill level. Chimney tray 107 is correspondingly large to be able to absorb also relatively large amounts of regenerated methanol in case of variations in the amount of the raw synthesis gas feed and thus variations in the amount of the circulating methanol. Regenerated methanol withdrawn from the chimney tray 107 is supplied via conduit 110 to a pump 104 for compression to the pressure prevailing in the absorption apparatus (for example 60 bar). The compressed regenerated methanol finally passes via conduit 112 into the indirect heat exchanger 102 and is therein cooled against cold methanol from conduit 101 to the low temperature required for the absorption (for example 50 C.). The cryogenic methanol is subsequently supplied to the absorption apparatus (not shown) via conduit 113 for renewed absorption of gas constituents from raw synthesis gas. Indirect heat exchanger 102 is shown as a single heat exchanger in FIG. 1. In practice said heat exchanger is typically a group of two or more heat exchangers, wherein one or more of these heat exchangers may have a dedicated coolant supply. The abovementioned heat exchangers must be configured for the high pressures (for example 60 bar) prevailing in the absorption apparatus.

[0075] FIG. 2 shows a schematic flow diagram of a process or an apparatus 200 for regenerating a laden scrubbing medium such as is known from the prior art. In the comparative example of FIG. 2 methanol is used as the scrubbing medium and regenerated using an apparatus for hot regeneration.

[0076] Reference numerals for elements in FIG. 1 having the same tens and units in the numeral as in FIG. 2 correspond to identical elements. For example the conduit 101 in FIG. 1 corresponds to the conduit 201 in FIG. 2. The hundreds in the reference numeral indicate the number of the respective figure.

[0077] The process/the apparatus 200 according to FIG. 2 differs from the process/the apparatus 100 according to FIG. 1 in that a second pump 214 and an additional conduit 215 are used. In the comparative example of FIG. 2 regenerated methanol withdrawn from the regeneration apparatus 205 via conduit 210 is supplied to a pump 204 in which the regenerated methanol is precompressed to an intermediate pressure (for example 10 bar). After cooling in heat exchanger 202 the precompressed methanol is compressed by pump 214 to the high pressure required for the absorption (for example 60 bar) and supplied to an absorption apparatus (not shown) via conduit 215.

[0078] FIG. 3 shows a schematic flow diagram of a process or an apparatus 300 for regenerating a laden scrubbing medium according to one working example of the invention. In the inventive example of FIG. 3 methanol is used as the scrubbing medium and regenerated using an apparatus for hot regeneration.

[0079] Via conduit 301 methanol laden with at least hydrogen sulfide (H.sub.2S) and hydrogen cyanide (HCN) is supplied from an absorption apparatus (not shown) and initially preheated against regenerated methanol from regeneration apparatus 305 in indirect heat exchanger 302. The laden methanol subsequently passes into heat exchanger 317 where it is preheated against regenerated methanol from regeneration apparatus 305 in a further heat exchanger stage before it is supplied to the regeneration apparatus 305 via conduit 313. Regeneration apparatus 305 is in the form of a stripping column for hot regeneration and comprises a reboiler 306, a chimney tray 307 and an overhead condenser (not shown). Laden methanol is largely freed of H.sub.2S and HCN in the regeneration apparatus 305 using methanol vapours produced by the reboiler 306. Abovementioned gas constituents not desired in the synthesis gas exit the regeneration apparatus 305 via conduit 308 together with methanol vapours not completely condensed by the overhead condenser. Once the methanol vapours have been condensed out of the H.sub.2S- and HCN-containing acid gas mixture in a separator the acid gas mixture is supplied to a Claus plant for recovery of sulfur (not shown).

[0080] Accumulating in the lower region of the regeneration apparatus 305 is methanol enriched with water which is withdrawn via conduit 309 and supplied to a distillation apparatus for methanol-water separation.

[0081] Regenerated methanol freed of all acid gases accumulates on chimney tray 307. In the context of the invention chimney tray 307 is also referred to as the sump of the regeneration apparatus. The fill level on chimney tray 307 is controlled via the fill level control apparatus 311. The fill level control apparatus 311 controls the amount of regenerated methanol withdrawn from the regeneration apparatus via conduit 310. If the synthesis gas feed and thus the circulating amount of methanol is increased for example a greater amount of regenerated methanol per unit time is withdrawn via conduit 310 to keep constant the fill level on the chimney tray 307. Fill level control apparatus 311 controls the amount to be removed via conduit using an actuated device, in this case control valve 321, which is in communication with fill level control apparatus 311 via a control circuit 316. Regenerated methanol withdrawn via conduit 310 is pre-cooled against laden methanol from conduit 303 in the indirect heat exchanger 317, passes via conduit 318 into a further heat exchanger 319 and finally via the conduits 322 and 323 and control valve 321 into intermediate vessel 320. Intermediate vessel 320 is configured for standard pressure or slight positive pressure as the operating pressure (for example 2 bar). Intermediate vessel 320 is optionally thermally insulated, i.e. provided on its outside with an insulating layer, in order that the pre-cooled regenerated methanol in the intermediate vessel 320 ideally does not undergo any warming. To check the fill level, intermediate vessel 320 is equipped with a fill level measuring apparatus 315. Intermediate vessel 320 is suitable for long-term storage of regenerated methanol and is therefore made of a material suitable therefor.

[0082] Due to the presence of the intermediate container 320 in conjunction with the components 311, 316 and 321 of the control apparatus, regeneration apparatus 305, in particular the region around the chimney tray 307 or sump, is smaller than regeneration apparatuses 105, 205 of the comparative examples.

[0083] Pre-cooled, regenerated methanol is withdrawn from intermediate vessel 320 via conduit 314 and compressed to the pressure prevailing in the absorption apparatus (for example 60 bar) using the pump 304. The compressed methanol is subsequently supplied via conduit 312 to heat exchanger 302 in which against laden methanol from conduit 301 it is cooled further to the temperature prevailing in the absorption apparatus. The cryogenic, regenerated methanol finally passes via conduit 324 into the absorption apparatus in order therein to absorb undesired gas constituents from raw synthesis gas once more.

[0084] Since the compression of the regenerated methanol is carried out by pump 304 and pump 304 is arranged downstream of the intermediate vessel 320 the heat exchangers 317 and 319 arranged upstream of the intermediate vessel 320 may advantageously be operated at standard pressure or slight positive pressure.

[0085] FIG. 4 shows a schematic flow diagram of a process or an apparatus 400 for regenerating a laden scrubbing medium according to a further working example of the invention. In the inventive example of FIG. 4 methanol is used as the scrubbing medium and regenerated using an apparatus for hot regeneration. Compared to the process mode of FIG. 3 after exiting the absorption apparatus the laden scrubbing medium is supplied initially to a flash vessel as the decompression stage and subsequently to a reabsorber before it is supplied to the regeneration apparatus.

[0086] Methanol laden at least with carbon dioxide (C.sub.2), hydrogen sulfide (H.sub.2S) and hydrogen cyanide (HCN) is supplied from an absorption apparatus (not shown) via conduit 401 and decompressed into the flash vessel (decompression stage) 426 via pressure reduction valve 425. Gases desorbed in the decompression exit the flash vessel 426 via conduit 427. Since the gases in conduit 427 contain valuable gases such as H.sub.2 and CO they are recompressed via a compressor and supplied to the absorption apparatus once more. The cold gases withdrawn via conduit 427 may further be used for cooling elsewhere in the gas scrubbing process by indirect heat transfer with a further fluid. Examples include the cooling of the raw synthesis gas supplied to the absorption apparatus or the additional cooling of regenerated methanol from conduit 410 or from conduit 414, wherein the cooling takes place in the heat exchangers 417/402.

[0087] The methanol laden with a reduced gas concentration as a result of the decompression is withdrawn from the flash vessel via conduit 428 and supplied to a reabsorber 429. In the reabsorber 429 CO.sub.2 is expelled (stripped) from the laden methanol by nitrogen supplied via conduit 432, it being unavoidable that certain amounts of hydrogen sulfide (H.sub.2S) are co-expelled. Co-expelled H.sub.2S gas is reabsorbed by laden methanol supplied via conduit 428. A substream of the hot regenerated methanol from conduit 424 may also be used for reabsorption (not shown). The gas stream containing mainly CO.sub.2 and N.sub.2 exits the reabsorber via conduit 430. Methanol laden mainly with H.sub.2S is withdrawn from the reabsorber 429 via conduit 431 and in indirect heat exchanger 402 preheated against regenerated methanol from regeneration apparatus 405. The laden methanol subsequently passes into heat exchanger 417 where it is preheated against regenerated methanol from regeneration apparatus 405 in a further heat exchanger stage before it is supplied to the regeneration apparatus 405 via conduit 413. Regeneration apparatus 405 is in the form of a stripping column for hot regeneration and comprises a reboiler 406, a chimney tray 407 and an overhead condenser (not shown). Laden methanol is largely freed of H.sub.2S in the regeneration apparatus 405 using methanol vapours produced by the reboiler 406. Abovementioned gas constituents not desired in the synthesis gas exit the regeneration apparatus 405 via conduit 408 together with methanol vapours not completely condensed by the overhead condenser. Once the methanol vapours have been condensed out of the H.sub.2S- and HCN-containing acid gas mixture in a separator the acid gas mixture is supplied to a Claus plant for recovery of sulfur (not shown).

[0088] Accumulating in the lower region of the regeneration apparatus 405 is methanol enriched with water which is withdrawn via conduit 409 and supplied to a distillation apparatus for methanol-water separation.

[0089] Regenerated methanol freed of all acid gases accumulates on chimney tray 407. In the context of the invention chimney tray 407 is also referred to as the sump of the regeneration apparatus. The fill level on chimney tray 407 is controlled via the fill level control apparatus 411. Fill level control apparatus 411 controls the amount of regenerated methanol withdrawn from the regeneration apparatus via conduit 410. If the synthesis gas feed and thus the circulating amount of methanol is increased for example a greater amount of regenerated methanol per unit time is withdrawn via conduit 410 to keep constant the fill level on the chimney tray 407. Fill level control apparatus 411 controls the amount to be removed via conduit 410 using an actuated device, in this case control valve 421, which is in communication with fill level control apparatus 411 via a control circuit 416. Regenerated methanol withdrawn via conduit 410 is pre-cooled against laden methanol from conduit 403 in the indirect heat exchanger 417, passes via conduit 418 into a further heat exchanger 419 and finally via the conduits 422 and 423 and control valve 421 into intermediate vessel 420. Intermediate vessel 420 is configured for standard pressure or slight positive pressure as the operating pressure (for example 2 bar). Intermediate vessel 420 is optionally thermally insulated, i.e. provided on its outside with an insulating layer, in order that the pre-cooled regenerated methanol in the intermediate vessel 420 ideally does not undergo any warming. To check the fill level, intermediate vessel 420 is equipped with a fill level measuring apparatus 415. Intermediate vessel 420 is suitable for long-term storage of regenerated methanol and is therefore made of a material suitable therefor.

[0090] Although laden methanol is regenerated in an apparatus for hot regeneration 405 relatively small residual amounts of H.sub.2S (trace amounts) nevertheless pass into the intermediate vessel 430 with the regenerated methanol. The use of the flash vessel 426 has the result that this H.sub.2S amount is yet further reduced and this may advantageously be accounted for in the choice of material for the intermediate vessel 420.

[0091] Due to the presence of the intermediate container 420 in conjunction with the components 411, 416 and 421 of the control apparatus, regeneration apparatus 405, in particular the region around the chimney tray 407 or sump, is smaller than regeneration apparatuses 105, 205 of the comparative examples.

[0092] Pre-cooled, regenerated methanol is withdrawn from intermediate vessel 420 via conduit 414 and compressed to the pressure prevailing in the absorption apparatus (for example 60 bar) using the pump 404. The compressed methanol is subsequently supplied via conduit 412 to heat exchanger 402 in which against laden methanol from conduit 431 it is cooled further to the temperature prevailing in the absorption apparatus. The cryogenic, regenerated methanol finally passes via conduit 424 into the absorption apparatus in order therein to absorb undesired gas constituents from raw synthesis gas once more.

[0093] Since the compression of the regenerated methanol is carried out by pump 404 and pump 404 is arranged downstream of the intermediate vessel 420 the heat exchangers 417 and 419 arranged upstream of the intermediate vessel 420 may advantageously be operated at standard pressure or slight positive pressure.

[0094] The following numerical example shows a comparison between the embodiments of FIG. 3 and of FIG. 4 in respect of residual amounts (trace amounts) of valuable gases (H.sub.2, CO) and H.sub.25 detectable in the regenerated methanol of the intermediate vessel. The numerical example further shows the differences between the amounts of heat transferred in the main heat exchangers (302 and 317 in FIG. 3; 402 and 417 in FIG. 4) and the coolant consumption between the different absorption stages of the absorption apparatus.

[0095] In both examples (FIG. 3 and FIG. 4) the raw synthesis gas supplied to the absorption apparatus has the same composition according to the following table. A partially shifted raw synthesis gas is concerned, i.e. a portion of the carbon monoxide present in the raw synthesis gas was reacted with water to afford hydrogen and carbon dioxide in a water gas shift reaction.

TABLE-US-00001 Component in raw synthesis gas Proportion in mol % CO 27.80 H.sub.2 43.01 CO.sub.2 28.47 N.sub.2 0.38 Ar 0.10 H.sub.2S 0.23 COS 0.01

[0096] The following values were calculated using the simulation software Aspen Plus. To aid comparison the numerical values calculated for the example of FIG. 3 were normalized, i.e. set to 100%. The volume flow of raw synthesis gas supplied to the absorption apparatus is 1 000 000 Nm.sup.3/h at an absorption pressure of 34 bar in both examples.

TABLE-US-00002 FIG. 3 example FIG. 4 example (without flash vessel) (with flash vessel) Residual loading of valuable 100% 5% gases (H.sub.2, CO) in regenerated methanol* H.sub.2 + CO recovery 100% 143% Residual loading of H.sub.2S in 100% 75% regenerated methanol* H.sub.2S in Claus gas 100% 128% Main heat exchanger 100% 94% Coolant consumption 100% 86% *as detectable in intermediate vessel

[0097] The numerical values show the unexpected advantages of the inventive embodiment according to FIG. 4 (with flash vessel) compared to the inventive embodiment according to FIG. 3 (without flash vessel).

[0098] The use of a flash vessel (decompression stage) lowers the residual loading of valuable gases detectable in the regenerated methanol of the intermediate vessel significantly by a factor of 20. Correspondingly, somewhat larger amounts of H.sub.2 and CO are recovered (43% increase). It is reiterated at this juncture that the abovementioned numbers relate to the residual loadings of valuable gases introduced into the regeneration apparatus (305, 405). Simultaneously, the residual loading of H.sub.2S introduced into the intermediate vessel is reduced by 25% as a result of which the corresponding amount of H.sub.2S in the Claus gas exiting the regeneration apparatus via the conduits 308/408 increases by 28%.

[0099] The use of a flash vessel has the further unexpected effect that compared to the main heat exchangers 302 and 317 the main heat exchangers 402 and 417 transfer an amount of heat that is 6% lower. Simultaneously, the coolant consumption of the coolant evaporators that cool the CO.sub.2-laden methanol between the individual absorption stages of the absorption apparatus decreases.

[0100] Embodiments of the invention are described with reference to different types of subject-matter. In particular, certain embodiments are described with reference to process claims while other embodiments are described with reference to apparatus claims. However, it will be apparent to a person skilled in the art from the description hereinabove and hereinbelow that unless otherwise stated in addition to any combination of features belonging to one claim type, any combination of features relating to different types of subject matter or claim types may also be contemplated. All features may be combined to achieve synergistic effects which go beyond simple summation of the technical features.

[0101] While the invention has been represented and described in detail in the drawings and the preceding description, such a representation and description shall be considered elucidatory or exemplary and non-limiting. The invention is not limited to the disclosed embodiments. Other variations of the disclosed embodiments may be understood and carried out by those skilled in the art of the field of the claimed invention through study of the drawings, the disclosure and the dependent claims. Accordingly, it is intended to embrace all such alternatives, modifications, and variations as fall within the spirit and broad scope of the appended claims.

[0102] The present invention may suitably comprise, consist or consist essentially of the elements disclosed and may be practiced in the absence of an element not disclosed. Furthermore, if there is language referring to order, such as first and second, it should be understood in an exemplary sense and not in a limiting sense. For example, it can be recognized by those skilled in the art that certain steps can be combined into a single step.

[0103] The singular forms a, an and the include plural referents, unless the context clearly dictates otherwise.

[0104] Comprising in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of comprising). Comprising as used herein may be replaced by the more limited transitional terms consisting essentially of and consisting of unless otherwise indicated herein.

[0105] Providing in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary.

[0106] Optional or optionally means that the subsequently described event or circumstances may or may not occur. The description includes instances where the event or circumstance occurs and instances where it does not occur.

[0107] Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such a range is expressed, it is to be understood that another embodiment is from the one particular value and/or to the other particular value, along with all combinations within said range.

[0108] All references identified herein are each hereby incorporated by reference into this application in their entireties, as well as for the specific information for which each is cited.

LIST OF REFERENCE SIGNS

[0109] 100 Process/apparatus

[0110] 101 Conduit

[0111] 102 Heat exchanger

[0112] 103 Conduit

[0113] 104 Pump

[0114] 105 Regeneration apparatus

[0115] 106 Reboiler

[0116] 107 Chimney tray

[0117] 108 Conduit

[0118] 109 Conduit

[0119] 110 Conduit

[0120] 111 Fill level measuring apparatus

[0121] 112 Conduit

[0122] 113 Conduit

[0123] 200 Process/apparatus

[0124] 201 Conduit

[0125] 202 Heat exchanger

[0126] 203 Conduit

[0127] 204 Pump

[0128] 205 Regeneration apparatus

[0129] 206 Reboiler

[0130] 207 Chimney tray

[0131] 208 Conduit

[0132] 209 Conduit

[0133] 210 Conduit

[0134] 211 Fill level measuring apparatus

[0135] 212 Conduit

[0136] 213 Conduit

[0137] 214 Pump

[0138] 215 Conduit

[0139] 300 Process/apparatus

[0140] 301 Conduit

[0141] 302 Heat exchanger

[0142] 303 Conduit

[0143] 304 Pump

[0144] 305 Regeneration apparatus

[0145] 306 Reboiler

[0146] 307 Chimney tray

[0147] 308 Conduit

[0148] 309 Conduit

[0149] 310 Conduit

[0150] 311 Fill level control apparatus

[0151] 312 Conduit

[0152] 313 Conduit

[0153] 314 Conduit

[0154] 315 Fill level measuring apparatus

[0155] 316 Control circuit

[0156] 317 Heat exchanger

[0157] 318 Conduit

[0158] 319 Heat exchanger

[0159] 320 Intermediate vessel

[0160] 321 Control valve

[0161] 322 Conduit

[0162] 323 Conduit

[0163] 324 Conduit

[0164] 400 Process/apparatus

[0165] 401 Conduit

[0166] 402 Heat exchanger

[0167] 403 Conduit

[0168] 404 Pump

[0169] 405 Regeneration apparatus

[0170] 406 Reboiler

[0171] 407 Chimney tray

[0172] 408 Conduit

[0173] 409 Conduit

[0174] 410 Conduit

[0175] 411 Fill level control apparatus

[0176] 412 Conduit

[0177] 413 Conduit

[0178] 414 Conduit

[0179] 415 Fill level measuring apparatus

[0180] 416 Control circuit

[0181] 417 Heat exchanger

[0182] 418 Conduit

[0183] 419 Heat exchanger

[0184] 420 Intermediate vessel

[0185] 421 Control valve

[0186] 422 Conduit

[0187] 423 Conduit

[0188] 424 Conduit

[0189] 425 Pressure reduction valve

[0190] 426 Flash vessel

[0191] 427 Conduit

[0192] 428 Conduit

[0193] 429 Reabsorber

[0194] 430 Conduit

[0195] 431 Conduit

[0196] 432 Conduit