CN107250327A - Method for producing methane and electric power - Google Patents
Method for producing methane and electric power Download PDFInfo
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- CN107250327A CN107250327A CN201680010902.0A CN201680010902A CN107250327A CN 107250327 A CN107250327 A CN 107250327A CN 201680010902 A CN201680010902 A CN 201680010902A CN 107250327 A CN107250327 A CN 107250327A
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- steam
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- synthesis gas
- methane
- carbon
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 11
- 238000000034 method Methods 0.000 claims abstract description 41
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 28
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 28
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 22
- 230000008569 process Effects 0.000 claims abstract description 12
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims description 13
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 7
- 239000005864 Sulphur Substances 0.000 claims description 7
- 229920006395 saturated elastomer Polymers 0.000 claims description 7
- 238000011144 upstream manufacturing Methods 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 4
- 238000006477 desulfuration reaction Methods 0.000 claims description 2
- 230000023556 desulfurization Effects 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 239000003054 catalyst Substances 0.000 description 10
- 238000009833 condensation Methods 0.000 description 9
- 230000005494 condensation Effects 0.000 description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 239000003292 glue Substances 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000006855 networking Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/04—Gasification
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/06—Heat exchange, direct or indirect
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/10—Recycling of a stream within the process or apparatus to reuse elsewhere therein
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
- C10L2290/148—Injection, e.g. in a reactor or a fuel stream during fuel production of steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/46—Compressors or pumps
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/48—Expanders, e.g. throttles or flash tanks
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/542—Adsorption of impurities during preparation or upgrading of a fuel
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
Method for producing methane and electric power comprises the following steps：Synthesis gas is produced from carbonaceous feed, and synthesis gas is carried out methanation in two or more methanators and is produced superheated steam in one or more superheaters, superheated steam is fed to back pressure turbine in the process to drive recycle compressor, and used all or part of steam in the turbine is added in methanation the possibility to reduce carbon formation and recycle compressor energy is saved.Electric power can be produced with relatively low price by this way.
Description
The present invention relates to the method for production methane and electric power.It is more particularly related to by superheated steam feed to
Turbine, and used steam is used for technique addition or heated, it is possible thereby to which the price lower than normal production prices is come
Produce electric power.
Steam turbine is the device for extracting heat energy from steam under pressure and doing mechanical work on rotating output shaft using it,
That is, turbine drives something, such as pump, compressor or generator using steam.Because turbine produces rotary motion,
It is particularly suitable for use in driving generator.Steam turbine is a kind of form of heat engine, and it is multiple by being used in steam expansion
Stage obtains most of improvement in terms of thermodynamic efficiency, and which results in closer to preferable reversible expansion process.
Non-condensing or back pressure turbine are most widely used for process steam application.By governor valve control pressure at expulsion, with suitable
The need for answering process steam pressure.This turbine is typically found in the oil plant for needing substantial amounts of low pressure process steam.
It is known from US 6.047.549A that there is combustion gas turbine, steam turbine and the Gas/Steam of mixing turbine
Power plant equipment.By using the appropriate networking of three turbine equipments, isothermal heat supply is realized with optimal Waste Heat Reuse
With the method except heat.Specifically, the used heat for the turbine set continuously arranged is used to produce high-pressure spray, it is to promote efficiency
Mode is used in back pressure turbine.
The A1 of US 2010/0263607 describe a kind of system for being used to produce steam for the turbine of generator.The system
Including receiving steam from boiler and making the superheater of steam superheating.Then make superheated steam by heat exchanger with by superheated steam
In a part of heat energy transfer into current.The temperature of superheated steam is reduced to the temperature for being suitable for turbine by this.In heat friendship
The water heated in parallel operation can be condensed water by turbine, and the water heated in a heat exchanger can be directed
To boiler, it is recycled into steam there.
A kind of production in low energy ammonia or methanol device using synthesis gas heat is disclosed in the A1 of US 2011/0120127
The method of raw supercritical steam.This method is related to reformation or partial oxidation stage, and suitable for the equipment bag of operation this method
Include at least one supercritical steam generator, at least one superheater, at least one back pressure turbine, at least one extract and
Condense turbine and at least one boiler feed pump.With it, energy-conservation and overall cost advantage can be realized, i.e., more preferably
Process economy.
Finally, multicomponent gasification, methanation and the power island that combination is disclosed in the A1 of US 2010/0170247 are steamed
Steam turbine system.Gasifying section includes recuperation of heat and designs and controlled for obtaining desired steam and the related of dry gas ratio
System, and methanation portion include first, second, and third methanator and with high pressure, middle pressure and low-pressure turbine and height
The related recuperation of heat that pressure energy-saving appliance is combined.Power island steam turbine includes high pressure, middle pressure and low-pressure turbine, and it has
The input being coupled with the output end of the superheater in methanation.The theme of the citation and subject of the present invention
Difference is that pressure turbine and recycle compressor are not connected to, and no steam is added to any methanation step
Enter in stream.
Difference of the invention with above-mentioned prior art is that it is used in the SNG methods of applicant, and wherein steam exists
Internal consumption is added to avoid carbon from being formed in process gas with hot gas, or by steam, is more specifically avoided " brilliant
The formation of palpus carbon ".In the process, SNG is produced by cheap carbon raw material such as coal, petroleum coke, biomass or waste and (substitutes day
Right gas).SNG is rich in methane, and it and can in an identical manner be allocated with natural gas used interchangeably.
Carbonaceous feed is carried out to SNG conversion with following several processing steps：
- by feed vaporization, to produce the gas rich in hydrogen and carbon monoxide；
- conversion, to adjust the ratio between hydrogen and carbon monoxide；
- sour gas is removed, wherein removing carbon dioxide and hydrogen sulfide in washing process；
- methanation, methane (SNG) is converted into by oxycarbide and hydrogen, is then dried and may be compressed to product SNG
Pipeline condition；
- oxygen for the gasification in air gas separation unit is produced, and
- reclaim sulphur from sour gas removal unit, its be most often by Claus units according to below equation
Hydrogen sulfide is converted into sulphur to complete：
If desired, sulphur then can be changed into the concentrated sulfuric acid in wet sulfuric acid (WSA) unit.
Methanation is such a process：Oxycarbide and hydrogen are wherein converted into by methane according to following reaction：
With
Balance between these reaction meetings and carbon monoxide as follows and carbon dioxide is coupled：
(2) and (3) both high exothermic heats are reacted, it discharges substantial amounts of reaction heat.For any industrial methane
For change technology, effective recovery of reaction heat is essential.
It is known that, according to operating condition and actual catalyst composition, catalyst can be formed from steam reformation field
Carbon.Carbon can be formed on a catalyst by methane, carbon monoxide or higher hydrocarbon.Forming carbon by methane and carbon monoxide can lead to
Following reaction is crossed to represent：
The carbon of formation depends on operating condition and catalyst.Generally, the carbon on Ni catalyst is the form of whisker carbon.It is described
Whisker carbon is described in the literature, see, for example, " Concepts in Syngas Manufacture " by J.Rostrup-
Nielsen and Lars J.Christiansen,Catalytic Science Series vol.10,2011,pages
233-235.As described above, the selection of catalyst and operating condition is it is determined whether form carbon.It is former according to so-called balanced gas
Reason, if thermodynamic prediction forms carbon after the balance of reaction (2)-(4) by one or more reaction (5)-(7), carbon will shape
Into.See, for example, the 247-252 pages of above-mentioned document.In this case, it is to avoid carbon formation means include reduction temperature and
The steam content that increase enters in the feed gas of reactor.
The heat discharged by above-mentioned methanation reaction is most effectively reclaimed as high pressure superheated steam.
The basic thought of the present invention is to be used for work by vapours charging charging to back pressure turbine and by used steam
Skill is added or heated.By such mode, electric power can be produced with relatively low price, because in case of heating,
It make use of 100% condensation energy.In the case of technique addition steam, by with adding saturated vapor and using condensation turbine
Machine is compared, it can be seen that the latter causes relatively low capacity usage ratio.
Therefore, the present invention relates to a kind of method for producing methane and electric power, this method comprises the following steps：With itself
Known mode produces synthesis gas from carbonaceous feed, and makes feed synthesis gas after being protected by the sulphur for desulfurization two
Methanation is carried out in individual or more methanator, wherein
- saturated vapor is produced in one or more boilers, and fed to one or more superheaters to convert
For superheated steam；
- feed at least a portion superheated steam to back pressure turbine, to drive recycle compressor, its compression comes from
A part for the effluent of last methanator；With
- used all or part of steam will be added in the turbine in methanation, with reduce carbon formation can
Energy property and the energy for saving recycle compressor.
The utilization of superheated steam is vital in the present invention.Superheated steam is (in the absolute pressure in absolute pressure
Temperature is determined under power) under temperature be higher than its evaporating point (boiling point) steam.
In the boiler, technique wasted energy (waste energy) is transferred in aqueous water to produce steam.In present invention side
In the boiler used in method, water is always at boiling point.Once reaching boiling point, the temperature of water just stops rising and keeps constant, directly
All evaporated to all water.Water enters steam condition, and the reception energy in the form of evaporation latent heat from liquid.As long as having
Aqueous water is present, then the temperature of steam is just identical with the temperature of aqueous water.Then, steam is referred to as saturated vapor.
When all water is all evaporated, any subsequent heat addition can all improve the temperature of steam.When steam is added
When heat exceedes saturated vapor level, it is referred to as superheated steam.
Industry is used to heat, dried or other operations usually using saturated vapor.Superheated steam is used almost exclusively for turbine
Machine is to drive generator, compressor, pump etc..
Back pressure turbine be used to drive recycle compressor.Generally, due to its relatively low power consumption, compressor drives
Dynamic device is electronic in SNG factories.Even so, power consumption of the invention is then lower, and actually it is zero.
Feed gas is preferably such gas, and the combined concentration of wherein hydrogen and oxycarbide is at least 60%.
The process of the present invention is shown in the drawings.Synthesis gas feeds (A) and preferably comprises at least 7 moles of %'s based on dry weight meter
The methane of methane, more preferably based at least 11 moles % of dry weight meter, the most preferably methane based at least 15 moles % of dry weight meter, make
It protects (SG) together with a small amount of water by sulphur, is followed by gas regulation reactor (GC).Water can be (but not necessarily
It is) high steam HP.A small amount of aqueous water can also be used, it then evaporates in the pipeline of reactor upstream.
In gas regulation reactor (GC), occurs transformationreation
Purpose is that temperature is increased into about 320 DEG C.Under relatively low inlet temperature, in the first methanator (M1)
In the presence of the risk for forming glue.Due to glue may also be formed because of high CO concentration, use gas regulation reactor (GC)
With " dual " advantage, because transformationreation reduces CO concentration.The quantity of steam for protecting (SG) upstream to add in sulphur is so
It is low, so that when entering SG, concentration is 0.01 to 1.00%, usually 0.3%.
Then adjusted gas is made to pass through two or more methanators.Embodiment bag shown in accompanying drawing
Include two methanators (M1 and M2).Using from methanation in boiler (B1 and B2) and steam superheater (S1 and S2)
The reaction heat of reactor, superheated steam or its at least a portion then be fed to turbine (T) to drive recycle compressor
(RC)。
In the method for the invention, steam pressure 30 bar preferably higher than feed gas pressure.
Used steam is fed to methanator from turbine to reduce the possibility of carbon formation.At possible point
After stream, the position in close proximity to the first methanator M1 (also likely to be present shift activity catalyst herein) upstream is by steam
It is added in system.By this way, the steam added will not be directly entered GC or M2.Between reactor GC and M1
It can be maximally effective that steam is added at position.When there is both transformation catalyst and methanation catalyst, then both are catalyzed
Agent is advantageously placed in the reactor of separation, that is, is respectively placed in GC and M1.The reactor of the separation before adjacent M1 with putting
The GC reactors put are operated together as the compound reactor of adiabatic operation.This compound reactor obtains special by applicant
Profit, referring to the 818B of GB 2 018.If there is no shift activity catalyst, then steam can be added to after shunting
In diformazan alkylation reactors M2.This selection can be saved more.Can be by a part of used steaming from back pressure turbine
Vapour is added in the technique stream of desulfurized step upstream.
By using steam by this way, at least three wonderful advantages are obtained：
1) by changing O/C ratios and H/C ratios in reactor, Carbon balance is directly moved；
2) the more steaminess to the turbine for driving compressor produces higher recycling, and this causes lower temperature again,
Thus process conditions are made away from carbon region；With
3) moved due to balancing at low temperature to methane, thus in reactor lower temperature produce higher synthesis gas to
The conversion ratio of methane.
Therefore, by producing high steam first and (it is with the pressure of reduction in back pressure turbine by a portion
Driving recycle compressor) in use, the steam or a portion for then reducing all pressure are added in technique, and straight
Connect the equipment of addition steam and otherwise the factory such as driven by power recycle compressor compares, can be with consumption of energy most
Smallization and the risk for reducing carbon formation.
It is further illustrated by the examples that follow the present invention.
Embodiment 1
This example compares three kinds of different situations, more specifically traditional SNG techniques (the first situation) and sheet
Two kinds of situations (second and the third situation) of the method based on back pressure turbine of invention.Second distinguishes with the third situation
It is referred to as " turbine situation " and " turbine situation in addition ".
In the case of the first of traditional SNG techniques, steam production is roughly the same with other two kinds of situations, and from first
The outlet temperature of methanator is 675 DEG C.The power consumption for driving recycle compressor is 1818 kilowatts.
In the latter case, the first methanator is made to carbon shape to the extra steam of gas regulation reactor feed
Into distance bring up to 15 DEG C.Identical with the first situation, the outlet temperature from the first methanator is 675 DEG C, but
The power consumption for driving recycle compressor is zero.
For the third situation (turbine situation in addition), the outlet temperature from the first methanator is from 675
690 DEG C are increased to, and the distance formed with carbon is still 10 DEG C.Likewise, the power consumption of driving recycle compressor is zero.
As a result summarize in table 1 below：
Table 1
| Normal condition | Turbine situation | Other turbine situation | |
| Steam is produced, t/h | 216.1 | 211.8 | 215.1 |
| Power consumption, kW | 1818 | 0 | 0 |
| Outlet temperature from the first methanator, DEG C | 675 | 675 | 690 |
| The distance formed with carbon, DEG C | 10 | 15 | 10 |
Embodiment 2
This embodiment illustrates the use of condensation turbine in the method according to the invention.More specifically, with using it
The back pressure turbine that middle effluent steam can be used further in technique is compared, and has used condensation turbine.Condense turbine from
The energy of maximum possible amount is obtained in steam, steam condensate is left.
Two kinds of situations (condensation turbine situation and the alternative condensation turbine using condensation turbine are tested
Situation).When compared with the back pressure turbine situation in embodiment 1, the two condensation turbine situations show, for basis
The embodiment of the back pressure turbine of the present invention, total balance of steam is best.
As a result it is summarised in table 2 below：
Table 2
| Condense turbine situation | Alternative condensation turbine situation | |
| Steam is produced, t/h | 209.2 | 205.4 |
| Power consumption, kW | 0 | 0 |
| Outlet temperature from the first methanator, DEG C | 675 | 675 |
| To the distance of carbon formation, DEG C | 10 | 15 |
These embodiments are clearly illustrated, with the recycling for being directly added into any equipment of steam and otherwise driving
Compressor is compared, and consumption of energy can be minimized simultaneously and be reduced the risk of carbon formation.
Claims (10)
1. a kind of method for producing methane and electric power, the described method comprises the following steps：In a way known from carbon
Matter charging production synthesis gas, and make feed synthesis gas (A) by being used for after the sulphur protection (SG) of desulfurization at two or more
Methanation is carried out in multiple methanators (M1, M2), wherein
- saturated vapor is produced in one or more boilers (B1, B2), and the saturated vapor is fed to one or more
Superheater (S1, S2) is to be converted into superheated steam；
- at least a portion superheated steam is fed to back pressure turbine (T), to drive recycle compressor (RC), it is described again
Recycle compressor compresses a part for the effluent from last methanator；With
- used all or part of steam will be added in the turbine in methanation, to reduce the possibility of carbon formation
And save the energy of recycle compressor.
2. according to the method described in claim 1, wherein the reaction heat from the methanator (M1, M2) is used for into institute
State in boiler (B1, B2) and the steam superheater (S1, S2), to produce superheated steam.
3. method according to claim 1 or 2, wherein being entered by the turbine (T) to driving recycle compressor (RC)
Expect more steaminess to obtain higher recycling.
4. method according to claim 3, wherein the higher recycling causes at the first methanator (M1)
In lower outlet temperature, thus process conditions are removed from carbon region.
5. method according to claim 1 or 2, wherein synthesis gas charging (A) is rubbed based on dry weight meter comprising at least 7
Your % methane.
6. method according to claim 5, wherein synthesis gas charging based on dry weight meter comprising at least 11 moles %
Methane.
7. method according to claim 6, wherein synthesis gas charging based on dry weight meter comprising at least 15 moles %
Methane.
8. high 30 bar of method according to claim 1 or 2, wherein vapour pressure ratio feed gas pressure.
9. high 60 bar of method according to claim 1 or 2, wherein vapour pressure ratio feed gas pressure.
10. method according to claim 1 or 2, wherein a part of from the back pressure turbine used is steamed
Vapour is added in the technique stream of desulfurized step upstream.
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| DKPA201500163 | 2015-03-18 | ||
| DKPA201500163 | 2015-03-18 | ||
| PCT/EP2016/055963 WO2016146815A1 (en) | 2015-03-18 | 2016-03-18 | A process for the production of methane and power |
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| US4410336A (en) * | 1982-02-24 | 1983-10-18 | Combustion Engineering, Inc. | Production of pipeline gas from coal |
| CN101649232A (en) * | 2009-08-25 | 2010-02-17 | 山东铁雄能源煤化有限公司 | Synthesis process of natural gas employing methanation of coke oven gas |
| CN101885994A (en) * | 2009-01-06 | 2010-11-17 | 通用电气公司 | Heat integration in coal gasification and methanation reaction process |
| CN101910380A (en) * | 2008-01-07 | 2010-12-08 | 通用电气公司 | Method and apparatus to facilitate substitute natural gas production |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2261308B1 (en) * | 2009-05-07 | 2013-06-19 | Haldor Topsøe A/S | Process for the production of natural gas |
| US8420031B2 (en) * | 2010-10-19 | 2013-04-16 | General Electric Company | System and method of substitute natural gas production |
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- 2016-03-18 WO PCT/EP2016/055963 patent/WO2016146815A1/en active Application Filing
- 2016-03-18 CN CN201680010902.0A patent/CN107250327A/en active Pending
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| US4410336A (en) * | 1982-02-24 | 1983-10-18 | Combustion Engineering, Inc. | Production of pipeline gas from coal |
| CN101910380A (en) * | 2008-01-07 | 2010-12-08 | 通用电气公司 | Method and apparatus to facilitate substitute natural gas production |
| CN101885994A (en) * | 2009-01-06 | 2010-11-17 | 通用电气公司 | Heat integration in coal gasification and methanation reaction process |
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