CA1241545A - Medium-load power generating station with an integrated coal gasification plant - Google Patents
Medium-load power generating station with an integrated coal gasification plantInfo
- Publication number
- CA1241545A CA1241545A CA000455348A CA455348A CA1241545A CA 1241545 A CA1241545 A CA 1241545A CA 000455348 A CA000455348 A CA 000455348A CA 455348 A CA455348 A CA 455348A CA 1241545 A CA1241545 A CA 1241545A
- Authority
- CA
- Canada
- Prior art keywords
- gas
- plant
- power generating
- heat exchanger
- hydrogen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000003245 coal Substances 0.000 title claims abstract description 60
- 238000002309 gasification Methods 0.000 title claims abstract description 42
- 239000007789 gas Substances 0.000 claims abstract description 263
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 258
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 91
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 91
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 51
- 239000001257 hydrogen Substances 0.000 claims abstract description 51
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000009826 distribution Methods 0.000 claims abstract description 20
- 238000000746 purification Methods 0.000 claims abstract description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000003860 storage Methods 0.000 claims abstract description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 28
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 18
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 15
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 14
- 239000001569 carbon dioxide Substances 0.000 claims description 14
- 150000002431 hydrogen Chemical class 0.000 claims description 11
- 238000009434 installation Methods 0.000 claims description 8
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 7
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 7
- 229920006395 saturated elastomer Polymers 0.000 claims description 7
- 239000000446 fuel Substances 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 4
- 239000002737 fuel gas Substances 0.000 claims description 4
- 239000000470 constituent Substances 0.000 claims description 2
- 238000005201 scrubbing Methods 0.000 claims 1
- 229910052760 oxygen Inorganic materials 0.000 abstract description 19
- 239000001301 oxygen Substances 0.000 abstract description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 18
- 238000005868 electrolysis reaction Methods 0.000 abstract description 15
- 239000000203 mixture Substances 0.000 description 7
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 230000009102 absorption Effects 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
- 230000000153 supplemental effect Effects 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000002844 continuous effect Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 150000002926 oxygen Chemical class 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Abstract of the Disclosure:
Medium-load power generating station with an integrated coal gasification plant, a gas turbine power generating station part connected to the coal gasification plant, a steam power gen-erating station part connected to the raw gas heat exchanger plant of the coal gasification plant, a methanol synthesis plant having a plurality of modules connected in parallel to each other, and a purified gas distribution system which connects the methanol synthesis plant to the gas turbine power generating station part and which includes a purified gas continuous flow interim storage plant and is connected on the gas side to the raw gas heat exchanger plant. The methanol synthesis plant is associated, for hydrogen enrichment, to a "cooler-saturator loop" which is connected to the raw gas heat exchanger plant and consists of the saturator, a converting plant, cooler and following gas purification plant. In one mode of operation, a water electrolysis plant is associated with the methanol synthesis plant and its hydrogen line is connected to the methanol synthesis plant, and its oxygen line is connected to the coal gasifier.
Medium-load power generating station with an integrated coal gasification plant, a gas turbine power generating station part connected to the coal gasification plant, a steam power gen-erating station part connected to the raw gas heat exchanger plant of the coal gasification plant, a methanol synthesis plant having a plurality of modules connected in parallel to each other, and a purified gas distribution system which connects the methanol synthesis plant to the gas turbine power generating station part and which includes a purified gas continuous flow interim storage plant and is connected on the gas side to the raw gas heat exchanger plant. The methanol synthesis plant is associated, for hydrogen enrichment, to a "cooler-saturator loop" which is connected to the raw gas heat exchanger plant and consists of the saturator, a converting plant, cooler and following gas purification plant. In one mode of operation, a water electrolysis plant is associated with the methanol synthesis plant and its hydrogen line is connected to the methanol synthesis plant, and its oxygen line is connected to the coal gasifier.
Description
~Z4154S
Background of the Invention Field of the Invention The invention relates to a medium-load power generating station with an integrated coal gasification plant, with a gas turbine generating station part connected to the coal gasification plant with a steam power generating station part connected to the raw gas heat exchanger plant of the coal gasification plant, with a methanol synthesis plant consisting of several parallel-connected modules, and with a purified gas distribution system which connects the methanol synthesis plant to the gas turbine power generating station part and which includes a purified gas continuous-flow interim storage plant and is connected on the gas side to the raw gas heat exchanger plant.
The subject of a related development by the applicant is a medium-load power generating station for generating electric ~241545 power and methanol, in which a combination gas turbine/steam power generating station and a methanol synthesis plant having a plurality ox modules which modules can be added into the stream separately, is connected via a purified gas distribution system, to a coal gasification plant. The waste heat of the raw gas is fed to the steam power generating station part via a raw gas heat exchanger plant and is utilized there. In this medium-load power generating station, the generated electric power can be adapted quickly to the instantaneous power demands of the electric network without the need of employing a further expensive secondary fuel for load peaks and without the need that in the event of a sudden load reduction or even load shedding due to a disturbance, a loss of fuel has to be toll erated. Instead, methanol is produced to a larger degree in this medium-load power generating station at times of reduced demand of electric power and excesses as well as shortfalls of pure gas are buffered by the purified gas continuous flow interim storage plant which is associated with the pure gas distribution system.
Therefore, the relatively more sluggish coal gasification plant can continue to be operated with.constant output independently of the prevailing load demands of the electric network.
Because the composition of the purified gas flowing toward the methanol synthesis plant is far from the stoichiometric .ratio required for the methanol synthesis, the synthesis gas ~2~1S45 returned in the methanol synthesis reactors of the individual modules must ye enriched with hydrogen in times of reduced energy demand to utilize the not completely reacted synthesis gas which can no longer be burned in the combustion chamber of the gas turbine. This hydrogen enrichment could be achieved by external feedi}ng-in of hydrogen.
Summary of the Invention An object of toe invention is to provide in a medium-load power generating station of the type mentioned at the outset, the hydrogen required for the hydrogen enrichment of the synthesis gas of the methanol synthesis plant from the power generating station itself in a most economical manner.
With the foregoing and other objects in view, there is provided in accordance with the invention a medium-load power generating plant with an integrated coal gasification plant comprising a a coal gasification plant for producing raw hot fuel gas-containing carbon monoxide and hydrogen, b) a raw gas heat exchanger installation having a first raw gas heat exchanger for indirect heat exchange between the hot raw gas from the coal gasification plant with feedwater to .. .
generate steam, c) a gas purifier for purifying the raw gas, d) a central purified gas distribution system, :~LZ4~54~
e) a purified gas supply line connected to the raw gas heat exchanger installation and passing into the central purified gas distribution system, f) a purified gas continuous-flow interim storage plant connected in parallel to the purified gas supply line, g) a gas turbine power generating plant connected to the coal gasification plant to receive fuel via the purified gas supply line, h) a methanol synthesis plant having parallel-connected modules for converting CO and H2 into methanol connected to the gas turbine power generating plant via the central purified gas distribution system, the combination therewith of i) a cooler-saturator loop connected to a gas line contain-ing carbon monoxide produced in said coal gasification plant and converting it into a gas richer in hydrogen, comprising a saturator wherein the gas is saturated with moisture, a con-verter wherein at least part of the carbon monoxide in the gas saturated with moisture is converted to hydrogen and carbon dioxide; a cooler for cooling the products from the converter, : 20 a gas purification plant for the removal of carbon dioxide and hydrogen sulfide, if any, from the gas from the cooler, and connecting means for passing said purified gas to the methanol synthesis plant for hydrogen enrichment of synthesis gas to be converted into methanol.
In accordance with the invention, there is provided a medium-load power generating plant with an integrated coal gasification plant comprising:
a) a coal gasification plant for producing raw hot fuel gas-containing carbon monoxide and hydrogen, b) a raw gas heat exchanger installation having a first raw gas heat exchanger for indirect heat exchange between the hot raw gas from the coal gasification plant with feedwater to generate s:team, c) a gas purifier for purifying the raw gas, d) a central purified gas distribution system, e) a purified gas supply line connected to the raw gas heat exchanger installation and passing into the central purified gas distribution system, f) a purified gas continuous-flow interim storage plant connected in parallel to the purified gas supply line, go a gas turbine power generating plant connected to the coal gasification plant to receive fuel via the purified gas supply line, h) a methanol synthesis plant having parallel-connected modules connected to the purified gas line to receive purified gas containing CO and H2 which is partially reacted in the modules to produce methanol and a methanol exhaust gas containing unreacted carbon monoxide.
i) a cooler-saturator loop connected to the methanol synthesis plant for treating methanol exhaust gas therefrom containing carbon monoxide and converting it into a gas richer ., ~24~545 in hydrogen, comprising a saturator wherein the gas is saturated with moisture, a converter wherein at least part of the carbon monoxide in the gas saturated with moisture is converted to hydrogen and carbon dioxide; a cooler for cooling the products from the converter, a gas purification plant for the removal of carbon dioxide and hydrogen sulfide, if any, from the gas from the cooler, and connecting means for passing said purified gas to the methanol synthesis plant for hydrogen enrich-ment of synthesis gas to be converted into methanol.
Other features which are considered as characteristic for the invention are set forth in the appended claims.
Although the invention is illustrated and described herein as embodied in a medium-load power generating station with an integrated coal gasification plant, it is nevertheless not intended to be limited to the details shown, since various modifications may be made therein without departing from the spirit of the invention and within the scope and range of equivalents of the claims.
Brief Description of the Drawings The invention, however, together with the additional objects and advantages thereof will be best understood from the following description when read in connection with the accompany-ing drawings, in which:
Figure 1 is a schematic presentation of a medium-load power generating station with an integrated coal gasification plant and a water electrolysis plant associated with the methanol synthesis plant, 124~545 FIG . 2 is a different medium-load power generating station with an integrated coal gasification plant and a so-called "cooler-saturator loop" associated with the methanol synthesis plant, and FIG. 3 is a variant for connecting the methanol synthesis plant of FIG.2 to the so-called "cooler-saturator loop".
Detailed Description of the Invention The invention relates to a medium-load power generating station with an integrated coal gasification plant with a gas turbine power generating station part connected to the coal gasification plant, with a steam power generating station part connected to the raw gas heat exchanger plant of the coal gasification plant and with a methanol synthesis plant. In such a medium-load power generating station, more methanol is generated in times of reduced power demand. The remaining synthesis gas which is now no longer burned in the gas turbine, has a composition far short of that desired and the objective is to bring the composition closer to the stoichiometric ratio required for the methanol synthesis. To this end. the methanol synthesis plant is assoçiated for the purpose of hydrogen enrichment, with a so-called cooler-saturator loop which is connected to the raw gas heat exchanger plant and includes a saturator, a converting plant, coolers and a gas purification plant connected thereto. Furthermore, a water electrolysis plant can also be as;sociated with the methanol synthesis plant ~Z41545 with a hydrogen line from the electrolysis plant connected via a compressor to the methanol synthesis plant. Fossil fuels are suitable for use with a medium-load power generating station according to the invention.
In a medium-load power generating station of the type mentioned at the outset, the methanol synthesis plant, according to the invention, is therefore associated for the hydrogen enrichment with a so-called "cooler-saturator loop" which is connected to the raw gas heat exchanger plant and consists of saturator, conversion plant, cooler and a following gas purification plant. In 'such a cooler-saturator loop hydrogen and carbon dioxide are generated by introduction of steam into the synthe-sis gas and subsequent conversion of the synthesis gas/steam mixture. After separating the carbon dioxide, the remaining synthesis gas, enriched with hydrogen, is returned to the methanol synthesis plant.
As an alternative, a water electrolysis plant in which water is converted to hydrogen and oxygen by electrolysis, the hydrogen is connected by a hydrogen line to the methanol synthesis plant and the oxygen by an oxygen line to the coal gasification plant, thereby associating the water electrolysis plant with the medium-load power generating station and with the methanol synthesis plant. In such an arrangement, the electric power generated in excess at tlmes of reduced power demands', can be .
124154~
utilized in the water electrolysis plant for generating hydro-gen and oxygen gases. The hydrogen can be used immediately for the enrichment of the synthesis gas of the methanol synthesis plant. The simultaneously generated oxygen can be fed to the coal gasifi~r. The oxygen there substitutes for a part of the oxygen which would otherwise be supplied by the air separation plant, reducing the output of the latter and thereby saving energy.
Further details of the invention will be explained with the aid of two embod3ment examples shown in the drawings.
In the presentation of FIG. 1, the superimposed assemblies of the medium-load power generating station 1 are framed by dashed lines. These are coal gasifier 2, a raw gas heat exchanger plant 3, a was purification plant 4, a central purified gas distribution system 5 with an integrated pressurizer and storage plant (not shown here for the sake of clarity), a combination power generating station 8 consisting of a gas turbine power generating station part 6 and a steam power generating station part 7, and a methanol synthesis plant 9.
The coal gasification plant 2 includes a coal gasifier 10, and air separation plant 11 with at least one additional air compressor 12 preceding the air sepàration plant, and a further oxygen gas compressor 14 which is arranged in the oxygen line 13 leading from the air separation plant 11 to the coal 1;;~4154S
~asifier 10. The raw gas heat exchanger plant 3 arranged in the gas stream from the coal gasifier 10 includes a first heat exchanger 15 for generating high-pressure steam, a second raw gas/purified gas heat exchanger 16 and a third heat exchanger 17 or generating low-pressure steam. Finally, a control cooler 18 is provided in the raw-gas heat exchanger plant 3.
The gas purification plant 4 following the raw gas heat exchanger plant includes a raw gas scrubber 19 as well as a hydrogen sulfide absorption and sulfur extraction plant 20. To the purified gas line 21 leaving the hydrogen sulfide absorp-tion and sulfur extraction plant 20 are connected the purified gas distribution system 5, the methanol synthesis plant 9 and, via the raw gas/purified gas heat exchanger 16, the gas turbine power generating plant part 6.
The gas turbine power generating station part 6 includes a combustion chamber 22, a gas turbine 23 and one generator 24 and one air compressor 25 driven by the gas turbine 23.
The exhaust gas line 26 of the gas turbine 23 is connected to a waste heat boiler 27. Its steam line 28 is connected to the high-pressure part 29 of a steam` turbine 31 consisting of a high-pressure part 29 and a low-pressure part 30. generator 32 is coupled to the steam turbine 31. The 1.ow-pressure part 30 of the steam turbine 31 is followed by a condenser 33, a condensate pump 34, a feedwater tank 35 as well as several ... .
feedwater pumps 36, 37, 38, 39. The combustion chamber 22 of the gas turbine as well as the air separation plant 11 of the coal gasification plant 2 are connected to the air compressor 25 driven by the gas turbine 23. A water electrolysis plant 40, wherein water is converted to oxygen and hydrogen, is associated with the coal gasification plant. The oxygen line 41 of the electrolysis plant 40 is connected in parallel to the oxygen line 13 of the.air separation plant 11 to the coal gasifier 10. The hydrogen line 42 of the water electrolysis plant 40 is connected via a hydrogen gas compressor 43 to the methanol synthesis plant 9.
In the operation of the medium-load power generating station 1, the air separation plant 11 is supplied with air by the air compressor 25 driven by the gas turbine 23 as well as by the supplemental air compressor 12. The oxygen of the air sepa-ration plant is forced into the coal gasifier 10 by the gas compressor 14. Coal is gasified with oxygen and fed-in process steam in the coal gasifier 10 to form raw gas. The hot raw gas discharged from gasifier 10 at a temperature of 800 to 1600C
gives off its heat in the heat exchanger plant 3, being utilized in part to generaté high-pressure steam in the first heat exchanger 15. In the second raw gas/purified gas heat exchanger 16, the purified gas flowing toward the combustion chamber 22 o the gas turbine power generating plant part 6 is preheated by the raw gas. In the third heat exchanger 17, 11 ' 12~:1545 additional pleat from the raw gas is utilized to generate low-pressure steam which can be fed to the low pressure part 30 of the steam turbine 31 or can be used as process steam. The control cooler 18 cools the raw gas to a defined temperature before it enters the raw gas scrubber 19. The pressure mainte-nance which takes place in the purified gas line 21 leaving the gas purification plant 4 is accomplished via the purified gas distribution system 5 wi-th an integrated purified gas continu-ous flow interim storage plant.
The methanol synthesis plant 9, which is subdivided into several modules which can separately be cut-in or cut-out of operation, remains switched-on in the operation of the medium load power generating station 1 at nominal load with at least one module which operates in continuous flow operation. At so-called low-load times when less electric power is given off to the network, the gas turbine power generating station part 6 is cut back first. The excess purified gas is consumed by running the modules of the methanol synthesis plant 9 which happened to be in operation at higher capacity, or by adding further modules. Thus, the coal gasification plant 2 can be continued to be operated in the optimum range for gasification of coal. The water electrolysis plant 40 can be set in opera-tion with part of the excess steam while the output of the gas turbine power generating station part is reduced at the same time. The hydrogen produced by electrolysis can be fed through , lZ41545 line 42 into the methanol synthesis plant 9 by means of the compressor 43. Thereby, the composition of the pure gas fed into the methanol synthesis plant or of the synthesis gas recirculating in the methanol synthesis plant is brought closer to the stoichiometric ratio required for the methanol synthe-sis. The oxygen produced at the same time in the water electrolysis plant 40 is fed to the coal gasifier 10. This oxygen substitutes for part of the oxygen from the air sepa-ration plant 11. As a result, the output of the air separation plant 11 can be reduced. In this manner, the quantity of methanol generated in times of reduced power demand can be increased by modifying the synthesis gas composition normally going to the methanol synthesis plant to a composition closer to the stoichiometric ratio by the addition of hydrogen gen-erated by excess electric power. By this procedure the entire amount of active constituents, namely carbon monoxide and hydrogen in the purified gas generated at nominal load of the coal gasifier 10 which is not needed by the gas turbine power generating station part 6 is completely converted into methanol.
A further increase in methanol quantity is produced if addi-tionally, hydrocarbon containing gas from an external source (not shown) is cracked to form synthesis gas and this gas is fed into the methanol synthesis plant. In this case, the entire electric power of the network can be fed to the water ~Z41545 electrolysis plant 40 in an extreme case of complete separation of the mediu~/low power generation station 1 from this network.
Since in this mode of operation of the medium/low power gen-erating station, only a small amount of the purified gas generated- by the coal gasifier is available for methanol synthesis, there is inadequate hydrogen to effect complete reaction of the carbon monoxide in the purified gas to methanol by methanol synthesis, and this hydrogen is available from the hydrocarbon containing gas fed-in from the external source to substantially complete the methanol synthesis. The coal gasification plant 2 is continued to be operated at nominal load regardless of whether the combination power generating station 8 consisting of a gas turbine part 6 and a steam generating station part 7 is continued to be operated at nominal load at times of reduced power demands or whether its output is reauced in such times. The purified gas produced in excess and/or at the same time, synthesis gas from the cracking of additional hydrocarbon containing gas is converted into methanol.
The medium-load power generating station 44 of the embodiment example shown in FIG. 2 consists of a coal gasification plant 45, a raw gas heat exchanger plant 46, a gas purification plant 47, a combination power generating station 48 including a gas turbine power generating station part and a steam power gen-erating station part, a methanol synthesis plant 49 and a 12~1545 central purified/gas distribution system 50 with a purified gas continuous-flow interim storage plant (not shown here for the sake of clarity) connected in parallel to the purified gas line 51. The coal gasification plant 45 includes a coal gasifier 52, and air separation plant 53, a supplemental air compressor 54 preceding the air separation plant 53, and an oxygen gas compressor 56 arranged in the oxygen line 55 to the coal gasifier 52. Also, the.raw gas heat exchanger plant 46 associ-ated with the raw gas stream issuing from the coal gasifier 52 includes a heat exchanger 57 for generating steam, a raw gas/purified gas heat exchanger 58, a heat exchanger 59 for generating-hot water, and a control cooler 60. The gas puri-fication plant 47 following the raw gas heat exchanger plant 46 includes a raw gas scrubber 61 and a hydrogen sulfide absorp-tion and sulfur extraction plant 62.
To the purified gas line 51 leaving the gas purification plant 47 is connected, similar to the embodiment example of FIG. 1, to the central purified gas distribution system 50, the methanol synthesis plant 49 and, via the purified gas/raw gas heat exchanger 58, to the combination power generating station 48. The latter'is designed'as'shown in detail in the er~odi-ment example of FIG. 1.
.
In a modification of the embodiment example of FIG. 1, a so-called ~cooler-saturator loop" 63 is connected to the lZ41545 methanol synthesis plant 49. The loop includes a saturator 64, a converter 65, a heat exchanger 66, a cooler 67 and a gas purification plant 68. The synthesis gas enriched in the cooler-saturator loop with hydrogen is returned via a recircu-lation line 69 to the methanol synthesis plant 49 and is fed to the synthesis xeactor (not shown for clarity) of the methanol synthesis plant.
In the operation of the medium-load power generating station 44 raw gas is generated in the coal gasifier 52 with the oxygen of the air separation plant 53 and with steam in a manner similar to that described in connection with embodiment example of FIG.
1. Raw gas issuing from coal gasifier 52 is cooled in the following raw gas heat exchanger plant 46 and is purified in the gas purification plant 47. The combination power generat-ing station 48 including a gas turbine power generating station part and a steam power generating station part is operated by burning in the gas turbine the purified gas from the gas distribution system 50 after first preheating the purified gas in the raw gas/purified gas heat exchanger 58. Also, the high-pressure steam generated in the first heat exchanger 57 of the raw gas heat exchanger plant 46 is fed to the steam turbine of the steam power generating station part. The synthesis gas partially reacted in the modules of the methanol synthesis plant 49, but which gas contains unreacted carbon monoxide, is conducted into the saturator 64 with steam by means of hot ~241545 water which is taken from the third heat exchanger 59 of the raw gas heat exchanger plant 46, thereby saturating the synthe-sis wit)h moisture. The mixed gas obtainea in this manner is converted in the following converting plant 65 by reaction of the carbon monoxide with water to give carbon dioxide and hydrogen. The exhaust gas of the converting plant 65 is cooled in a first heat exchanger 66, where the cooling water warrned up in this exchanger is fed for further heating into the third heat exchanger 59 of the raw gas heat exchanger plant 4~. The thus pr~cooled exhaust gas of the converting plant 65 is further cooled in a cooler 67 connected to the cooler loop 70 and the cooled exhaust gas from cooler 67 introduced into the gas purification plant 68. In this gas purification plant, the carbon dioxide is washed out and the remaining gas enriched with hydrogen is returned as synthesis gas via the recircu-lation line 69 to the methanol synthesis plant 49. There, it is fed to a synthesis reactor which is in operation.
If desired, the exhaust gas of the converting plant may be treated in a gas separation plant to obtain a fraction rich in hydrogen. Also, the purified gas flowing initially into the methanol æynthesis plant may be enriched with hydrogen via the cooler-saturator loop instead of making synthesis gas from the synthesis reactor of the methanol synthesis plant, in order that the synthesis gas approach a stoichiometric ratio for the methanol generation.
124~S4S
This synthesis gas enriched with hydrogen could then be fed to the methanol synthesis plant and recirculated there through the individual synthesis reactors until it is completely reacted to methancl, except, of course, for the inert gas residues. The connection of the methanol synthesis plant 71 for this type of pre-enrichment of the purified gas with hydrogen is shown in the embodiment example of FIG. 3. It is seen here that the purified gas line 72 is first fed to the otherwise unchanged cooler-saturator loop 73 and only the exhaust gas which is enriched with hydrogen and freed of carbon aioxide is fed to the converting plant behind the gas purification plant via the recirculating line 74 into the methanol synthesis plant 71.
The output of the gas turbine can also be reduced or the turbine can be switched off at times when less power is fed into the electric network. The purified gas which under these conditions i5 available in larger quantity, can be converted via the methanol synthesis plant into methanol while the synthesis gas is enriched with hydrogen. The,heat produced in larger quantity in the third heat exchanger 58 of the raw gas heat exchanger plant 46 can be utilized for further saturation of the pure gas and in some circumstances, for the additional decomposition of externally introduced hydrocarbon containing gas. Due to the increase of the synthesis gas production, more methanol can be produced.
Background of the Invention Field of the Invention The invention relates to a medium-load power generating station with an integrated coal gasification plant, with a gas turbine generating station part connected to the coal gasification plant with a steam power generating station part connected to the raw gas heat exchanger plant of the coal gasification plant, with a methanol synthesis plant consisting of several parallel-connected modules, and with a purified gas distribution system which connects the methanol synthesis plant to the gas turbine power generating station part and which includes a purified gas continuous-flow interim storage plant and is connected on the gas side to the raw gas heat exchanger plant.
The subject of a related development by the applicant is a medium-load power generating station for generating electric ~241545 power and methanol, in which a combination gas turbine/steam power generating station and a methanol synthesis plant having a plurality ox modules which modules can be added into the stream separately, is connected via a purified gas distribution system, to a coal gasification plant. The waste heat of the raw gas is fed to the steam power generating station part via a raw gas heat exchanger plant and is utilized there. In this medium-load power generating station, the generated electric power can be adapted quickly to the instantaneous power demands of the electric network without the need of employing a further expensive secondary fuel for load peaks and without the need that in the event of a sudden load reduction or even load shedding due to a disturbance, a loss of fuel has to be toll erated. Instead, methanol is produced to a larger degree in this medium-load power generating station at times of reduced demand of electric power and excesses as well as shortfalls of pure gas are buffered by the purified gas continuous flow interim storage plant which is associated with the pure gas distribution system.
Therefore, the relatively more sluggish coal gasification plant can continue to be operated with.constant output independently of the prevailing load demands of the electric network.
Because the composition of the purified gas flowing toward the methanol synthesis plant is far from the stoichiometric .ratio required for the methanol synthesis, the synthesis gas ~2~1S45 returned in the methanol synthesis reactors of the individual modules must ye enriched with hydrogen in times of reduced energy demand to utilize the not completely reacted synthesis gas which can no longer be burned in the combustion chamber of the gas turbine. This hydrogen enrichment could be achieved by external feedi}ng-in of hydrogen.
Summary of the Invention An object of toe invention is to provide in a medium-load power generating station of the type mentioned at the outset, the hydrogen required for the hydrogen enrichment of the synthesis gas of the methanol synthesis plant from the power generating station itself in a most economical manner.
With the foregoing and other objects in view, there is provided in accordance with the invention a medium-load power generating plant with an integrated coal gasification plant comprising a a coal gasification plant for producing raw hot fuel gas-containing carbon monoxide and hydrogen, b) a raw gas heat exchanger installation having a first raw gas heat exchanger for indirect heat exchange between the hot raw gas from the coal gasification plant with feedwater to .. .
generate steam, c) a gas purifier for purifying the raw gas, d) a central purified gas distribution system, :~LZ4~54~
e) a purified gas supply line connected to the raw gas heat exchanger installation and passing into the central purified gas distribution system, f) a purified gas continuous-flow interim storage plant connected in parallel to the purified gas supply line, g) a gas turbine power generating plant connected to the coal gasification plant to receive fuel via the purified gas supply line, h) a methanol synthesis plant having parallel-connected modules for converting CO and H2 into methanol connected to the gas turbine power generating plant via the central purified gas distribution system, the combination therewith of i) a cooler-saturator loop connected to a gas line contain-ing carbon monoxide produced in said coal gasification plant and converting it into a gas richer in hydrogen, comprising a saturator wherein the gas is saturated with moisture, a con-verter wherein at least part of the carbon monoxide in the gas saturated with moisture is converted to hydrogen and carbon dioxide; a cooler for cooling the products from the converter, : 20 a gas purification plant for the removal of carbon dioxide and hydrogen sulfide, if any, from the gas from the cooler, and connecting means for passing said purified gas to the methanol synthesis plant for hydrogen enrichment of synthesis gas to be converted into methanol.
In accordance with the invention, there is provided a medium-load power generating plant with an integrated coal gasification plant comprising:
a) a coal gasification plant for producing raw hot fuel gas-containing carbon monoxide and hydrogen, b) a raw gas heat exchanger installation having a first raw gas heat exchanger for indirect heat exchange between the hot raw gas from the coal gasification plant with feedwater to generate s:team, c) a gas purifier for purifying the raw gas, d) a central purified gas distribution system, e) a purified gas supply line connected to the raw gas heat exchanger installation and passing into the central purified gas distribution system, f) a purified gas continuous-flow interim storage plant connected in parallel to the purified gas supply line, go a gas turbine power generating plant connected to the coal gasification plant to receive fuel via the purified gas supply line, h) a methanol synthesis plant having parallel-connected modules connected to the purified gas line to receive purified gas containing CO and H2 which is partially reacted in the modules to produce methanol and a methanol exhaust gas containing unreacted carbon monoxide.
i) a cooler-saturator loop connected to the methanol synthesis plant for treating methanol exhaust gas therefrom containing carbon monoxide and converting it into a gas richer ., ~24~545 in hydrogen, comprising a saturator wherein the gas is saturated with moisture, a converter wherein at least part of the carbon monoxide in the gas saturated with moisture is converted to hydrogen and carbon dioxide; a cooler for cooling the products from the converter, a gas purification plant for the removal of carbon dioxide and hydrogen sulfide, if any, from the gas from the cooler, and connecting means for passing said purified gas to the methanol synthesis plant for hydrogen enrich-ment of synthesis gas to be converted into methanol.
Other features which are considered as characteristic for the invention are set forth in the appended claims.
Although the invention is illustrated and described herein as embodied in a medium-load power generating station with an integrated coal gasification plant, it is nevertheless not intended to be limited to the details shown, since various modifications may be made therein without departing from the spirit of the invention and within the scope and range of equivalents of the claims.
Brief Description of the Drawings The invention, however, together with the additional objects and advantages thereof will be best understood from the following description when read in connection with the accompany-ing drawings, in which:
Figure 1 is a schematic presentation of a medium-load power generating station with an integrated coal gasification plant and a water electrolysis plant associated with the methanol synthesis plant, 124~545 FIG . 2 is a different medium-load power generating station with an integrated coal gasification plant and a so-called "cooler-saturator loop" associated with the methanol synthesis plant, and FIG. 3 is a variant for connecting the methanol synthesis plant of FIG.2 to the so-called "cooler-saturator loop".
Detailed Description of the Invention The invention relates to a medium-load power generating station with an integrated coal gasification plant with a gas turbine power generating station part connected to the coal gasification plant, with a steam power generating station part connected to the raw gas heat exchanger plant of the coal gasification plant and with a methanol synthesis plant. In such a medium-load power generating station, more methanol is generated in times of reduced power demand. The remaining synthesis gas which is now no longer burned in the gas turbine, has a composition far short of that desired and the objective is to bring the composition closer to the stoichiometric ratio required for the methanol synthesis. To this end. the methanol synthesis plant is assoçiated for the purpose of hydrogen enrichment, with a so-called cooler-saturator loop which is connected to the raw gas heat exchanger plant and includes a saturator, a converting plant, coolers and a gas purification plant connected thereto. Furthermore, a water electrolysis plant can also be as;sociated with the methanol synthesis plant ~Z41545 with a hydrogen line from the electrolysis plant connected via a compressor to the methanol synthesis plant. Fossil fuels are suitable for use with a medium-load power generating station according to the invention.
In a medium-load power generating station of the type mentioned at the outset, the methanol synthesis plant, according to the invention, is therefore associated for the hydrogen enrichment with a so-called "cooler-saturator loop" which is connected to the raw gas heat exchanger plant and consists of saturator, conversion plant, cooler and a following gas purification plant. In 'such a cooler-saturator loop hydrogen and carbon dioxide are generated by introduction of steam into the synthe-sis gas and subsequent conversion of the synthesis gas/steam mixture. After separating the carbon dioxide, the remaining synthesis gas, enriched with hydrogen, is returned to the methanol synthesis plant.
As an alternative, a water electrolysis plant in which water is converted to hydrogen and oxygen by electrolysis, the hydrogen is connected by a hydrogen line to the methanol synthesis plant and the oxygen by an oxygen line to the coal gasification plant, thereby associating the water electrolysis plant with the medium-load power generating station and with the methanol synthesis plant. In such an arrangement, the electric power generated in excess at tlmes of reduced power demands', can be .
124154~
utilized in the water electrolysis plant for generating hydro-gen and oxygen gases. The hydrogen can be used immediately for the enrichment of the synthesis gas of the methanol synthesis plant. The simultaneously generated oxygen can be fed to the coal gasifi~r. The oxygen there substitutes for a part of the oxygen which would otherwise be supplied by the air separation plant, reducing the output of the latter and thereby saving energy.
Further details of the invention will be explained with the aid of two embod3ment examples shown in the drawings.
In the presentation of FIG. 1, the superimposed assemblies of the medium-load power generating station 1 are framed by dashed lines. These are coal gasifier 2, a raw gas heat exchanger plant 3, a was purification plant 4, a central purified gas distribution system 5 with an integrated pressurizer and storage plant (not shown here for the sake of clarity), a combination power generating station 8 consisting of a gas turbine power generating station part 6 and a steam power generating station part 7, and a methanol synthesis plant 9.
The coal gasification plant 2 includes a coal gasifier 10, and air separation plant 11 with at least one additional air compressor 12 preceding the air sepàration plant, and a further oxygen gas compressor 14 which is arranged in the oxygen line 13 leading from the air separation plant 11 to the coal 1;;~4154S
~asifier 10. The raw gas heat exchanger plant 3 arranged in the gas stream from the coal gasifier 10 includes a first heat exchanger 15 for generating high-pressure steam, a second raw gas/purified gas heat exchanger 16 and a third heat exchanger 17 or generating low-pressure steam. Finally, a control cooler 18 is provided in the raw-gas heat exchanger plant 3.
The gas purification plant 4 following the raw gas heat exchanger plant includes a raw gas scrubber 19 as well as a hydrogen sulfide absorption and sulfur extraction plant 20. To the purified gas line 21 leaving the hydrogen sulfide absorp-tion and sulfur extraction plant 20 are connected the purified gas distribution system 5, the methanol synthesis plant 9 and, via the raw gas/purified gas heat exchanger 16, the gas turbine power generating plant part 6.
The gas turbine power generating station part 6 includes a combustion chamber 22, a gas turbine 23 and one generator 24 and one air compressor 25 driven by the gas turbine 23.
The exhaust gas line 26 of the gas turbine 23 is connected to a waste heat boiler 27. Its steam line 28 is connected to the high-pressure part 29 of a steam` turbine 31 consisting of a high-pressure part 29 and a low-pressure part 30. generator 32 is coupled to the steam turbine 31. The 1.ow-pressure part 30 of the steam turbine 31 is followed by a condenser 33, a condensate pump 34, a feedwater tank 35 as well as several ... .
feedwater pumps 36, 37, 38, 39. The combustion chamber 22 of the gas turbine as well as the air separation plant 11 of the coal gasification plant 2 are connected to the air compressor 25 driven by the gas turbine 23. A water electrolysis plant 40, wherein water is converted to oxygen and hydrogen, is associated with the coal gasification plant. The oxygen line 41 of the electrolysis plant 40 is connected in parallel to the oxygen line 13 of the.air separation plant 11 to the coal gasifier 10. The hydrogen line 42 of the water electrolysis plant 40 is connected via a hydrogen gas compressor 43 to the methanol synthesis plant 9.
In the operation of the medium-load power generating station 1, the air separation plant 11 is supplied with air by the air compressor 25 driven by the gas turbine 23 as well as by the supplemental air compressor 12. The oxygen of the air sepa-ration plant is forced into the coal gasifier 10 by the gas compressor 14. Coal is gasified with oxygen and fed-in process steam in the coal gasifier 10 to form raw gas. The hot raw gas discharged from gasifier 10 at a temperature of 800 to 1600C
gives off its heat in the heat exchanger plant 3, being utilized in part to generaté high-pressure steam in the first heat exchanger 15. In the second raw gas/purified gas heat exchanger 16, the purified gas flowing toward the combustion chamber 22 o the gas turbine power generating plant part 6 is preheated by the raw gas. In the third heat exchanger 17, 11 ' 12~:1545 additional pleat from the raw gas is utilized to generate low-pressure steam which can be fed to the low pressure part 30 of the steam turbine 31 or can be used as process steam. The control cooler 18 cools the raw gas to a defined temperature before it enters the raw gas scrubber 19. The pressure mainte-nance which takes place in the purified gas line 21 leaving the gas purification plant 4 is accomplished via the purified gas distribution system 5 wi-th an integrated purified gas continu-ous flow interim storage plant.
The methanol synthesis plant 9, which is subdivided into several modules which can separately be cut-in or cut-out of operation, remains switched-on in the operation of the medium load power generating station 1 at nominal load with at least one module which operates in continuous flow operation. At so-called low-load times when less electric power is given off to the network, the gas turbine power generating station part 6 is cut back first. The excess purified gas is consumed by running the modules of the methanol synthesis plant 9 which happened to be in operation at higher capacity, or by adding further modules. Thus, the coal gasification plant 2 can be continued to be operated in the optimum range for gasification of coal. The water electrolysis plant 40 can be set in opera-tion with part of the excess steam while the output of the gas turbine power generating station part is reduced at the same time. The hydrogen produced by electrolysis can be fed through , lZ41545 line 42 into the methanol synthesis plant 9 by means of the compressor 43. Thereby, the composition of the pure gas fed into the methanol synthesis plant or of the synthesis gas recirculating in the methanol synthesis plant is brought closer to the stoichiometric ratio required for the methanol synthe-sis. The oxygen produced at the same time in the water electrolysis plant 40 is fed to the coal gasifier 10. This oxygen substitutes for part of the oxygen from the air sepa-ration plant 11. As a result, the output of the air separation plant 11 can be reduced. In this manner, the quantity of methanol generated in times of reduced power demand can be increased by modifying the synthesis gas composition normally going to the methanol synthesis plant to a composition closer to the stoichiometric ratio by the addition of hydrogen gen-erated by excess electric power. By this procedure the entire amount of active constituents, namely carbon monoxide and hydrogen in the purified gas generated at nominal load of the coal gasifier 10 which is not needed by the gas turbine power generating station part 6 is completely converted into methanol.
A further increase in methanol quantity is produced if addi-tionally, hydrocarbon containing gas from an external source (not shown) is cracked to form synthesis gas and this gas is fed into the methanol synthesis plant. In this case, the entire electric power of the network can be fed to the water ~Z41545 electrolysis plant 40 in an extreme case of complete separation of the mediu~/low power generation station 1 from this network.
Since in this mode of operation of the medium/low power gen-erating station, only a small amount of the purified gas generated- by the coal gasifier is available for methanol synthesis, there is inadequate hydrogen to effect complete reaction of the carbon monoxide in the purified gas to methanol by methanol synthesis, and this hydrogen is available from the hydrocarbon containing gas fed-in from the external source to substantially complete the methanol synthesis. The coal gasification plant 2 is continued to be operated at nominal load regardless of whether the combination power generating station 8 consisting of a gas turbine part 6 and a steam generating station part 7 is continued to be operated at nominal load at times of reduced power demands or whether its output is reauced in such times. The purified gas produced in excess and/or at the same time, synthesis gas from the cracking of additional hydrocarbon containing gas is converted into methanol.
The medium-load power generating station 44 of the embodiment example shown in FIG. 2 consists of a coal gasification plant 45, a raw gas heat exchanger plant 46, a gas purification plant 47, a combination power generating station 48 including a gas turbine power generating station part and a steam power gen-erating station part, a methanol synthesis plant 49 and a 12~1545 central purified/gas distribution system 50 with a purified gas continuous-flow interim storage plant (not shown here for the sake of clarity) connected in parallel to the purified gas line 51. The coal gasification plant 45 includes a coal gasifier 52, and air separation plant 53, a supplemental air compressor 54 preceding the air separation plant 53, and an oxygen gas compressor 56 arranged in the oxygen line 55 to the coal gasifier 52. Also, the.raw gas heat exchanger plant 46 associ-ated with the raw gas stream issuing from the coal gasifier 52 includes a heat exchanger 57 for generating steam, a raw gas/purified gas heat exchanger 58, a heat exchanger 59 for generating-hot water, and a control cooler 60. The gas puri-fication plant 47 following the raw gas heat exchanger plant 46 includes a raw gas scrubber 61 and a hydrogen sulfide absorp-tion and sulfur extraction plant 62.
To the purified gas line 51 leaving the gas purification plant 47 is connected, similar to the embodiment example of FIG. 1, to the central purified gas distribution system 50, the methanol synthesis plant 49 and, via the purified gas/raw gas heat exchanger 58, to the combination power generating station 48. The latter'is designed'as'shown in detail in the er~odi-ment example of FIG. 1.
.
In a modification of the embodiment example of FIG. 1, a so-called ~cooler-saturator loop" 63 is connected to the lZ41545 methanol synthesis plant 49. The loop includes a saturator 64, a converter 65, a heat exchanger 66, a cooler 67 and a gas purification plant 68. The synthesis gas enriched in the cooler-saturator loop with hydrogen is returned via a recircu-lation line 69 to the methanol synthesis plant 49 and is fed to the synthesis xeactor (not shown for clarity) of the methanol synthesis plant.
In the operation of the medium-load power generating station 44 raw gas is generated in the coal gasifier 52 with the oxygen of the air separation plant 53 and with steam in a manner similar to that described in connection with embodiment example of FIG.
1. Raw gas issuing from coal gasifier 52 is cooled in the following raw gas heat exchanger plant 46 and is purified in the gas purification plant 47. The combination power generat-ing station 48 including a gas turbine power generating station part and a steam power generating station part is operated by burning in the gas turbine the purified gas from the gas distribution system 50 after first preheating the purified gas in the raw gas/purified gas heat exchanger 58. Also, the high-pressure steam generated in the first heat exchanger 57 of the raw gas heat exchanger plant 46 is fed to the steam turbine of the steam power generating station part. The synthesis gas partially reacted in the modules of the methanol synthesis plant 49, but which gas contains unreacted carbon monoxide, is conducted into the saturator 64 with steam by means of hot ~241545 water which is taken from the third heat exchanger 59 of the raw gas heat exchanger plant 46, thereby saturating the synthe-sis wit)h moisture. The mixed gas obtainea in this manner is converted in the following converting plant 65 by reaction of the carbon monoxide with water to give carbon dioxide and hydrogen. The exhaust gas of the converting plant 65 is cooled in a first heat exchanger 66, where the cooling water warrned up in this exchanger is fed for further heating into the third heat exchanger 59 of the raw gas heat exchanger plant 4~. The thus pr~cooled exhaust gas of the converting plant 65 is further cooled in a cooler 67 connected to the cooler loop 70 and the cooled exhaust gas from cooler 67 introduced into the gas purification plant 68. In this gas purification plant, the carbon dioxide is washed out and the remaining gas enriched with hydrogen is returned as synthesis gas via the recircu-lation line 69 to the methanol synthesis plant 49. There, it is fed to a synthesis reactor which is in operation.
If desired, the exhaust gas of the converting plant may be treated in a gas separation plant to obtain a fraction rich in hydrogen. Also, the purified gas flowing initially into the methanol æynthesis plant may be enriched with hydrogen via the cooler-saturator loop instead of making synthesis gas from the synthesis reactor of the methanol synthesis plant, in order that the synthesis gas approach a stoichiometric ratio for the methanol generation.
124~S4S
This synthesis gas enriched with hydrogen could then be fed to the methanol synthesis plant and recirculated there through the individual synthesis reactors until it is completely reacted to methancl, except, of course, for the inert gas residues. The connection of the methanol synthesis plant 71 for this type of pre-enrichment of the purified gas with hydrogen is shown in the embodiment example of FIG. 3. It is seen here that the purified gas line 72 is first fed to the otherwise unchanged cooler-saturator loop 73 and only the exhaust gas which is enriched with hydrogen and freed of carbon aioxide is fed to the converting plant behind the gas purification plant via the recirculating line 74 into the methanol synthesis plant 71.
The output of the gas turbine can also be reduced or the turbine can be switched off at times when less power is fed into the electric network. The purified gas which under these conditions i5 available in larger quantity, can be converted via the methanol synthesis plant into methanol while the synthesis gas is enriched with hydrogen. The,heat produced in larger quantity in the third heat exchanger 58 of the raw gas heat exchanger plant 46 can be utilized for further saturation of the pure gas and in some circumstances, for the additional decomposition of externally introduced hydrocarbon containing gas. Due to the increase of the synthesis gas production, more methanol can be produced.
Claims (7)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A medium-load power generating plant with an integrated coal gasification plant comprising (a) a coal gasification plant for producing raw hot fuel gas-containing carbon monoxide and hydrogen, (b) a raw gas heat exchanger installation having a first raw gas heat exchanger for indirect heat exchange between the hot raw gas from the coal gasification plant with feedwater to generate steam, (c) a gas purifier for purifying the raw gas, (d) a central purified gas distribution system, (e) a purified gas supply line connected to the raw gas heat exchanger installation and passing into the central purified gas distribution system, (f) a purified gas continuous-flow interim storage plant connected in parallel to the purified gas supply line, (g) a gas turbine power generating plant connected to the coal gasification plant to receive fuel via the purified gas sup-ply line, (h) a methanol synthesis plant having parallel-connected modules for converting CO and H2 into methanol connected to the gas turbine power generating plant via the central purified gas distribution system, the combination therewith of (i) a cooler-saturator loop connected to a gas line containing carbon monoxide produced in said coal gasification plant and converting it into a gas richer in hydrogen, comprising a saturator wherein the gas is satruated with moisture, a con-verter wherein at least part of the carbon monoxide in the gas saturated with moisture is converted to hydrogen and carbon dioxide; a cooler for cooling the products from the converter a gas purification plant for the removal of carbon dioxide and hydrogen sulfide, if any, from the gas from the cooler, and con-necting means for passing said purified gas to the methanol syn-thesis plant for hydrogen enrichment of synthesis gas to be converted into methanol.
2. Medium-load power generating station according to claim 1, wherein the "cooler-saturator loop" is inserted into the purified gas line carrying the purified gas which leads to a module of the methanol synthesis plant.
3. Medium-load power generating station according to claim 1, inclucing another raw gas heat exchanger in the raw gas heat exchange plant for indirect heat exchange between the raw gas and water to heat the water and connecting means through which the saturator can be supplied with hot water from the heat exchanger of the raw gas heat exchanger plant.
4. Medium-load power generating station according to claim 1, wherein the gas purification plant comprises a carbon dioxide scrubbing plant to remove carbon dioxide.
5. Medium-load power generating station according to claim 1, wherein following the gas purification plant, a hydrogen separation plant is included in which a hydrogen rich fraction is separated by liquification of the less volatile gaseous constituents.
6. Medium-load power generating station according to claim 1 including steam connecting means from the first raw gas heat exchanger of the raw gas heat exchanger plant to the saturator for introducing steam into the saturator.
7. A medium-load power generating plant with an integrated coal gasification plant comprising (a) a coal gasification plant for producing raw hot fuel gas-containing carbon monoxide and hydrogen, (b) a raw gas heat exchanger installation having a first raw gas heat exchanger for indirect heat exchange between the hot raw gas from the coal gasification plant with feedwater to generate steam, (c) a gas purifier for purifying the raw gas, (d) a central purified gas distribution system, (e) a purified gas supply line connected to the raw gas heat exchanger installation and passing into the central purified gas distribution system, (f) a purified gas continuous-flow interim storage plant connected in parallel to the purified gas supply line, (g) a gas turbine power generating plant connected to the coal gasification plant to receive fuel via the purified gas supply line, (h) a methanol synthesis plant having parallel-connected modules connected to the purified gas line to receive purified gas containing CO and H2 which is partially reacted in the modules to produce methanol and a methanol exhaust gas containing unreacted carbon monoxide, (i) a cooler-saturator loop connected to the methanol synthesis plant for treating methanol exhaust gas therefrom containing carbon monoxide and converting it into a gas richer in hydrogen, comprising a saturator wherein the gas is saturated with moisture, a converter wherein at least part of the carbon monoxide in the gas saturated with moisture is converted to hydrogen and carbon dioxide; a cooler for cooling the products from the converter, a gas purification plant for the removal of carbon dioxide and hydrogen sulfide, if any, from the gas from the cooler, and connecting means for passing said purified gas to the methanol synthesis plant for hydrogen enrichment of synthesis gas to be converted into methanol.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000564343A CA1258773A (en) | 1983-05-31 | 1988-04-15 | Medium-load power generating station with an integrated coal gasification plant |
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19833319732 DE3319732A1 (en) | 1983-05-31 | 1983-05-31 | MEDIUM-POWER PLANT WITH INTEGRATED COAL GASIFICATION SYSTEM FOR GENERATING ELECTRICITY AND METHANOL |
| DEP3319732.6 | 1983-05-31 | ||
| DEP3327367.7 | 1983-07-29 | ||
| DE3332736 | 1983-07-29 |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000564343A Division CA1258773A (en) | 1983-05-31 | 1988-04-15 | Medium-load power generating station with an integrated coal gasification plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1241545A true CA1241545A (en) | 1988-09-06 |
Family
ID=25811177
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000455348A Expired CA1241545A (en) | 1983-05-31 | 1984-05-29 | Medium-load power generating station with an integrated coal gasification plant |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1241545A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6736955B2 (en) | 2001-10-01 | 2004-05-18 | Technology Convergence Inc. | Methanol production process |
-
1984
- 1984-05-29 CA CA000455348A patent/CA1241545A/en not_active Expired
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6736955B2 (en) | 2001-10-01 | 2004-05-18 | Technology Convergence Inc. | Methanol production process |
| US7714176B2 (en) | 2001-10-01 | 2010-05-11 | Technology Convergence Inc. | Methanol production process |
| US8188322B2 (en) | 2001-10-01 | 2012-05-29 | Technology Convergence Inc. | Methanol production process |
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