CN1155619A - Operation of integrated gasification combined cycle power generation systems at part load - Google Patents
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Abstract
An integrated gas turbine/air separation system is operated at or below full system load by feeding the air separation unit with air from a dedicated air feed compressor and optionally with extracted air from the gas turbine air compressor. When the gas turbine air compressor discharge drops below a selected pressure at part load conditions, the flow of extracted air to the air separation unit is discontinued and the air separation unit operates at constant pressure supplied only by the air feed compressor. This mode of operation is particularly useful in an integrated gasification combined cycle (IGCC) power generation system and allows the design of the oxygen and nitrogen product compressors such that the compressors operate at high efficiency during full load IGCC operation.
Description
The present invention relates to the operation of gasification combined cycle power generation systems, specifically, relate to when power generation systems when operating less than design load, the method that is used to operate gas turbine and air separation equipment.
With the generating of advanced person's combined vaporizing circulating pressure generation system than the generate electricity potentiality of the power cost that has more reduction and lower environmetal impact of the coal power power station with standard.In described AS, coal or other carbonaceous materials with oxygen gasified, are purified the gas that is produced, to obtain the low-sulfur inflammable gas.Utilize this inflammable gas in gas turbine generation system, to produce electric power, have the environmetal impact of reduction.(IGCC) the higher efficient of the advanced person's of system gas turbine, coal gasifying process and air separation system and the reliability that proved have evoked people in recent years to (GCC) increasing interest of technology of combined vaporizing circulation (gasification combined cycle) to be used for combined vaporizing circulation (integrated gasificationcombined cycle).Suitably uniting of three chief components of this of IGCC system to realizing that maximum operating efficiency and minimum power cost are necessary.
Article (in July, 1993, P1-18) proposition to be entitled as " CleanCoal Technologies for Gas Turbines " in GE Turbine State-of-the-Art Technology academic conference by D.M.Todd summarized to the generality of GCC and IGCC power generation systems in related domain.People such as A.K.Anand provide the summary of the design factor that relates to the IGCC system, paper is entitled as " New Technology Trends for Improved IGCC System Performance ", and this paper is delivered on the Intemational GasTurbine and Aeroengine Congress and Exposition that holds in the Houston, Texas 5-8 day June nineteen ninety-five.Relevant various United Technologies and the summary of the influence of GCC economy provided with the paper that is entitled as " Intergation of Texaco TQ Gasification with Elevated Pressure ASU " by people such as A.D.Rao, this paper is delivered in the 13rd the EPRI Conference on Gasification Power Plants meeting of holding in CA San Francisco 19-21 day in October, 1994.
In the paper that is entitled as " ImprovedIGCC Power Output and Economics Incorporating a Supplementary GasTurbine " that is to deliver in the 13rd the EPRIConference on Gasification Power Plants meeting that hold in CA San Francisco 19-21 day in October, 1994, people such as A.R.Smith have summarized gas turbine and several united modes of air separation equipment in IGCC technology.In a kind of pattern, the air separation equipment feeding air is to be provided by discrete compressor, then is compressed and is incorporated in the gas-turbine combustion chamber from the part nitrogen product of air separation equipment.The pattern of this associating nitrogen can allow operation IGCC system under the condition that the NOx of Gas Turbine Power output that increases and reduction forms.In another kind of operator scheme, associating nitrogen combines with the associating air, and the part feeding air that wherein enters into air separation equipment is provided by the gas of the extraction that comes from gas-turbine compressor.This another kind pattern is defined as the associating of air and nitrogen, and it can have bigger operating flexibility, and can in the operation IGCC systematic procedure higher optimization degree be arranged under with sub load and other off-design conditions.
Air and nitrogen associating gas turbine/air separation system are described in the following representational U. S. Patent:
U.S. Pat 3,731,495,4,019,314,4,224,045,4,557,735,4,697,415,5,081,845,5,386,686,5,406,786 and 5,410,869 and UK Patent Application UK 2067668A.
The power generation systems based on burning that comprises the IGCC system is limited by each operation period that is lower than the system design capacity, and this is owing to cause at ambient air temperature and/or to the variation of the circulation demand of electric power.Interim when these are operated, described system operates to be lower than design efficiency.Thereby the selection of equipment and must guarantee steady state operation under design capacity, and in off-design condition, sub load or close operation under (turndown) condition to the technological design of IGCC system.Above-mentioned air and nitrogen associating IGCC system is preferred because described system have maximum overall efficiency, particularly when described system also must be or close the potentiality of the operation when operating under the condition in non-design, sub load.
Below disclosed and set forth operating the demand of improving one's methods of advanced power generation systems by the present invention that appended claims limited, and specifically described in sub load or close under the condition improvement operation air and nitrogen associating gas turbine and air separation system.
The present invention relates to method with sub load operation associating gas turbine/air separation system, described method is included in pressurized air in the gas turbine air compressor, at least a portion gained pressurized air and fuel are burnt in gas-turbine combustion chamber, to form hot combustion products, this hot combustion products, described quencher Driven Compressor and the optional generator that drives expand in the gas turbine quencher.Air is separated into rich nitrogen and oxygen enriched product in low temp air fractionation system, wherein, the feeding air that enters into air separation equipment is provided by main air compressor, and optional is provided by the additional pressurized air from the gas turbine air compressor.Associating gas turbine/air separation system is operated with sub load, so that:
(a) when the gas turbine air compressor provides pressurized air with the given operation pressure greater than minimum air separation equipment feed pressure, air separation equipment with the essentially identical feed pressure operation of given operation pressure, and feeding air by main air compressor be provided to air separation equipment from the extention pressurized air of combustion gas turbine air compressor; Or
(b) when the gas turbine air compressor provides pressurized air with the given operation pressure that is equal to or less than minimum air separation equipment feed pressure substantially, air separation equipment is operated with the feed pressure that is substantially equal to minimum air separation equipment feed pressure, and the feeding air that is fed in the air separation equipment is provided by main air compressor, does not have the additional compressed air from the gas turbine air compressor.
Minimum air separation equipment feed pressure is 80-500 pound/square inch.
Main air compressor is operated with one of two kinds of patterns, so that
(a) when main air compressor with greater than the operation of the head pressure of minimum air separation equipment feed pressure the time, main air compressor with greater than the total compression ratio relatively of its minimal design be lower than the relative volume flow that sucks of its design maximum and operate; Or
(b) when main air compressor being substantially equal to head pressure when operation of minimum air separation equipment feed pressure, main air compressor basically with the total compression ratio relatively of its minimal design with or be lower than the relative volume flow that sucks of its design maximum and operate.
The total compression ratio relatively of the minimal design of main air compressor is relative with design maximum to suck volume flow and mainly produces when minimum air separation equipment feed pressure.Main air compressor is operation under 80-600 pound/square inch in head pressure.
Oxygen enriched product compresses in oxygen compressor, and this compressor is with any operation in two kinds of patterns, so that:
(a) when main air compressor is operated under the head pressure greater than minimum air separation equipment feed pressure, oxygen compressor is being lower than the total compression ratio relatively of its design maximum and is being lower than relative the suction under the volume flow of its design maximum and operates; Or
(b) when main air compressor basically with head pressure that minimum air separation equipment feed pressure equates under when operating, oxygen compressor basically the total compression ratio relatively of its design maximum with or be lower than relative the suction under the volume flow of its design maximum and operate.
The total compression ratio relatively of the design maximum of oxygen compressor is relative with design maximum suck volume flow occur in main air compressor basically with head pressure that minimum air separation equipment feed pressure equates under in the situation of operating.Oxygen compressor is operated under the head pressure of 120-2000 pound/square inch.
The inflammable gas that is used for gas-turbine combustion chamber can produce in the technology that is used to from the compressed oxygen enriched product vaporized carbon raw material of air separation equipment.
Can in nitrogen compressor, compress to the rich nitrogen product of small part to be used for the technology of vaporized carbon raw material.This nitrogen compressor is with any operation of two kinds of patterns, so that:
(a) when main air compressor is operated under the head pressure greater than minimum air separation equipment feed pressure, nitrogen compressor is being lower than the total compression ratio relatively of its design maximum and is being lower than relative the suction under the volume flow of its design maximum and operates; Or
(b) when main air compressor basically with head pressure that minimum air separation equipment feed pressure equates under when operating, nitrogen compressor basically the total compression ratio relatively of its design maximum with or be lower than relative the suction under the volume flow of its design maximum and operate.
The total compression ratio relatively of the design maximum of nitrogen compressor is relative with design maximum suck volume flow occur in main air compressor basically with head pressure that minimum air separation equipment feed pressure equates under in the situation when operating.Nitrogen compressor is operated under the head pressure of 50-2000 pound/square inch.
Can in nitrogen compressor, be compressed to the rich nitrogen product of small part, and be introduced in the gas-turbine combustion chamber.Under this kind selection, nitrogen compressor is with any operation of two kinds of patterns, so that:
(a) when main air compressor is operated under the head pressure greater than minimum air separation equipment feed pressure, nitrogen compressor is being lower than the total compression ratio relatively of its design maximum and is being lower than relative the suction under the volume flow of its design maximum and operates; Or
(b) when main air compressor basically with head pressure that minimum air separation equipment feed pressure equates under when operating, nitrogen compressor basically the total compression ratio relatively of its design maximum with or be lower than relative the suction under the volume flow of its design maximum and operate;
The total compression ratio relatively of the design maximum of nitrogen compressor and design maximum suck volume flow relatively and occur in the situation that main air compressor operates under identical with minimum air separation equipment feed pressure basically head pressure.Nitrogen compressor is operation under 120-2000 pound/square inch in head pressure.
By by separation equipment charging of the method for the invention design air and product compressor, gas turbine engine systems is operated under sub load, and only the total output consumption of air separation equipment is had small adverse effect.Yet, because main air compressor, oxygen product compressor and nitrogen product compressor are designed at the compression ratio of relative close limit and suck under the volume flow operate, thereby the compressor efficiency maximum when gas turbine engine systems full load design capacity (system's overwhelming majority time this moment is in operation), and the total output of air separation equipment consumes minimum.
Fig. 1 is the flow chart of the gasification combined cycle power generation systems of air and nitrogen associating.
Fig. 2 be or be lower than the performance chart of the gasification combined cycle power generation systems of application drawing 1 under the design capacity.
Fig. 3 is the compressor operation curve according to the air separation main air compressor of the compressor operation overall process of conventional practice operation.
Fig. 4 is the compressor operation curve according to the air separation products oxygen compressor of the compressor operation overall process of conventional practice operation.
Fig. 5 is the compressor operation curve of the air separation main air compressor of operating within the scope of the present invention.
Fig. 6 is the compressor operation curve of the air separation products oxygen compressor operated within the scope of the present invention.
The present invention relates to associating gas turbine/air separation system, wherein gas turbine and air separation equipment are by the delivery pipe of at least one air-flow a system and other system to be coupled together.For example, in air associating gas turbine/air separation system, some or all pressurized air chargings that is fed in the air separation equipment are provided in during the small part system operating time by gas-turbine compressor.In nitrogen associating gas turbine/air separation system, some or all be introduced in the gas-turbine combustion chamber in during the small part system operating time from the nitrogen product of air separation equipment.
In many applications, air and nitrogen are united and are preferred in combined vaporizing circulation (IGCC) system, this is because it has the potentiality of operating under maximum total capacity, especially in system in sub load or particularly like this when closing under the condition operation certain hour.Air and nitrogen associating IGCC technology are illustrated in Fig. 1, wherein ambient air 1 is compressed to 450 pounds/square inch from 150 pounds/square inch in gas turbine air compressor 3 under 600 °F～900 °F, this gas-turbine compressor 3 is typical axial flow adiabatic compressor.A part 7 and the fuel 9 of pressurized air 5 burn in gas-turbine combustion chamber 11, and to obtain combustion products logistics 13, general described burning is carried out under 2000～2800 °F.Fuel 9 is preferably vaporized fuel, and for example synthetic gas or rock gas are although also can use liquid fuel.Combustion products logistics 13 expands in gas turbine quencher 15, to produce axle power, this power driven compressor 3 and generator 17.Randomly, gas-turbine exhaust 19 is cooled off at heat recovery area 23 places at 0.2-2 pound/square inch and the boiler feed water 21 of 900～1100 following usefulness, and to produce steam 25, this steam 25 expands in steamer 27, to drive additional generator 29. Generator 17 and 29 can be united in an equipment.Last exhaust 31 is discharged in the atmosphere.
In common PRACTICE OF DESIGN, the amount of the gas 33 of extraction is fixed under given ambient air temperature as the percentage of the amount of whole air separation equipment charging demands.For example, the gas that term 50% is extracted out is meant that the gas 33 of extraction provides 50% of whole feeding airs to air separation equipment 39, and remaining 50% provided by main air compressor 33.100% gas of extracting out is meant that all feeding airs that are used for air separation equipment 39 are provided by gas-turbine compressor 3, does not then need from the air of main air compressor 43.
The cryogenic air separation process that is used for the ICGG system is known, and representational technology is described in U.S. Pat 4,224, in 045,5,081,845 and 5,224,336.The commercially available gasification system that is used for this application is by Texaco, Shell, and BG-Lurgi, Prenfio, HTW and Destec develop.Described raw material comprises coal, coke, decompression residuum and other heavy hydrocarbons.The part 59 of nitrogen product 49 is compressed into 50-2000 pound/square inch in nitrogen compressor 61, to obtain compressed nitrogen 63, this compressed nitrogen 63 is used for cleaning at gasification system 53, soot blowing and fortune coal.
The present invention is not limited to above-mentioned IGCC system, but can be used at any air associating gas turbine/air separation system that is lower than operation certain hour under the design capacity.In another kind of operator scheme,, do not use gasification system 53, and compressed oxygen product 52 provides with the pressure that is used for external application referring to Fig. 1.Randomly, nitrogen 59 is compressed in nitrogen compressor 61, be used for the product nitrogen gas 63 of external application with generation.Optional and preferably, nitrogen 65 is mixed with fuel 57, and acts as a fuel-nitrogen mixture 9 introducing firing chambers 11 in, perhaps in nitrogen compressor 67, compress, and directly introduce in 11 (not shown) of firing chamber.Fuel 57 is for example provided as natural gas by external source.Randomly, without generator 17 and 29, the operation association system is only for producing oxygen 52 and/or nitrogen 63.At this moment, compressor 3, firing chamber 11, turboexpander 15 and steamer 27 will carry out size and limit, only to provide air separation system required power.For any of above-mentioned selection, with sub load or when closing under the condition operating gas turbine engine systems, air separation equipment 39 will be operated in a manner described.
It is the process of a repetition with IGCC power station that the commerce of above-mentioned technology is used in design, and it relates to the optimal selection to gas turbine, air separation and gasification system, produces the required operational requirements of power to satisfy.These demands comprise as amount, every day and the seasonal power demand curve of the gas of the ambient temperature that is used for actual factory location, design maximum environmental temperature, design maximum power output, maximum gas turbine kindling temperature, extraction, with respect to relative importance and other demands of the investment of project operation cost.
Purpose of the present invention is exactly the preferred operation mode of decision Sq, the air separation equipment of bleeding and is used for the air separation equipment charging and the required design point of product compressor, this makes as the result of low power demand and/or ambient air temperature variation, in the change procedure of gas turbine output, best gas turbine/air separation equipment operation is arranged.
In the present invention, will under the condition of exporting less than design motivation, be defined as sub load or closing operation by the operation gas turbine.In the IGCC of Fig. 1 technology, two performance variables can reduce the power output of gas turbine.First is the increase of ambient air temperature in the above-mentioned variable, and the increase of this temperature reduces the density of feeding air 1, otherwise and reduce the mass flow rate of pressurized air 5 and the amount of pressurized air 33, it can be used for to air separation equipment 39 chargings.In order to operate being lower than under the maximum temperature limit of gas turbine quencher 15, the rate of heating of firing chamber 11 must reduce by the flow that reduces fuel 9.This has reduced the mass flow rate of combustion products 13 and the power output of quencher 15 conversely again.As a result, ambient air temperature rises 10 ℃ and can make the power output of typical IGCC system reduce by 4%.
Reduce by second decline that performance variable is power demand of the Gas Turbine Power output of IGCC system, this betides in typical power demand circulation every day.For example, the power demand at night to typical IGCC factory can be the 50-75% of demand on daytime.The seasonal variety of power demand also can take place.During reducing power demand, factory must be undertaken in sub load (promptly " closing ") operation down by air and the fuel flow rate that reduces gas-turbine combustion chamber.Gas turbine air compressor 3 can cut out or cut out by recirculated air in compressor assembly at the stator throttling intake air 1 of compressor 3 ingress by using.As a result, the mass flow rate and the pressure of compressor discharging 5 all reduce, and this has reduced the pressure of the gas 37 of the extraction that enters air separation equipment 39.This needs main air compressor 43 to operate under the head pressure that reduces conversely again, so air separation equipment 39 must operate under lower pressure, and this has reduced the pressure of oxygen product 47 and nitrogen product 49.Yet gasification system 53 is generally operated under fixation pressure, operates so oxygen compressor 51 and nitrogen compressor 61 must and be closed under the condition at the higher compression machine.Because need less fuel 57 when closing, so gasification system 53 needs less oxygen 47, thereby air separation equipment 39 needs less feeding air.
As stated before, present PRACTICE OF DESIGN is for the fixing speed of exhaust of given ambient air temperature and design load.In closing closed procedure, the charging of air separation equipment 39 continues to be provided by gas of extracting out 37 and compression feeding air 45.Therefore, main air compressor 43 must be designed to operate under the air-flow of wide range and compression ratio, so that cover full design capacity to the whole IGCC operating ranges between maximum the closing.Along with the operation pressure of air separation equipment 39 changes in this wide range, the suction pressure of oxygen and nitrogen compressor 51,61 and 67 also changes; Since the head pressure substantial constant of these compressors is so compression ratio changes significantly.In addition, along with the generation of closing, by the mass flow rate reduction of these compressor control.Under some operational circumstances under the combination that some low ambient temperature and IGCC close, have necessity and close main air compressor 43, and 37 pairs of air separation equipment chargings of gas by extracting out fully.
Fig. 2 has illustrated in the IGCC system control capacity of typical IGCC operation under the constant environment temperature, relation between gas turbine operation under full load and the sub load condition and air separation equipment operation.In this performance chart, the % that %, gas turbine (GT) air compressor head pressure and air separation equipment (ASU) operation pressure of gas turbine (GT) design inflammable gas capacity are loaded to gas turbine (GT) system design maps.The slope of these operating lines is features of design of special gas turbine engine systems and environmental conditions.At the A point, wherein A point representative design IGCC system Gas Turbine Power output, gas-turbine compressor 3 is operation under 190 pounds/square inch in head pressure, and air separation equipment 39 is operated under same pressure, this means that the head pressure of main air compressor 43 also is 190 pounds/square inch.Along with closing of gas turbine, with among the figure on Fig. 2 by operating under the defined output that reduces successively of B, C and D point, gas turbine air compressor head pressure will be by B, the C of middle graph and D point and is reduced, as a result, air separation equipment must be by the stress level operation down of some B, C among the figure below and reduction identical shown in the D point.Since the speed of exhaust is to determine according to common PRACTICE OF DESIGN, since and the whole air feeds that enter into air separation equipment reduce because of lower oxygen demand, so the mass flow rate of the gas 37 of the thruput of the air by main air compressor 43 and extraction will descend.
Therefore, the standard practices of flow that changes the gas 33 of pressure and extraction in whole gas turbine operating ranges needs will the compressor 43,51,61 and 67 relevant with air separation equipment 39 to be designed to operating in the wide range of the volume flow of D and compression ratio corresponding to the operating point A among Fig. 2.This is illustrated in Fig. 3, and Fig. 3 has provided the compressor operation curve of the main air compressor 43 of operating down in the gamut of the flow of the associating IGCC system operation of described A to D point corresponding to Fig. 2 and compression ratio.
In specification of the present invention and appended claims, if the difference of two pressure within 5 pounds/square inch, thinks then that they equate basically, and if variation in pressure be as the criterion less than about 1% by absolute pressure, then think this pressure substantial constant.Term " relatively compression ratio " means compression ratio at the compressor of any operating point divided by the compression ratio at selected design point.The actual volume at the place, suction port of compressor that term " sucks volume flow relatively " and is defined as at any operating point flows divided by flowing at the actual volume of selected design point at the place, suction port of compressor.Compressor operation curve for Fig. 3-6 of constant environment temperature is meant constant relative efficiency line, and constant relative efficiency is defined and makes actual compression efficiency divided by the efficient under fixing reference condition, n/n
RefEfficiency curve is the constraint of pulse curve by compression when higher compression ratios, as shown in the figure.When low relative suction volume flow, efficiency curve is subjected to the constraint of minimal flow curve, the compressor operation of minimal flow curve representative when compressor vanes is closed to as far as possible at utmost.When higher relative suction volume flow, efficiency curve is retrained by the maximum fluidity curve, the compressor operation performance of this maximum fluidity curve representative when stator reverses during at max-flow animal configuration.Neutrality as shown in the figure (neutral) stator opening curves is by reference point, and sucking volume flow relatively at this point is 1.0 with the total ratio of relative compression ratio.
Referring to Fig. 3, at the design operation capacity place of gas turbine engine systems, main air compressor 43 is in the operation of maximum fluidity position at the A point in maximum thruput and inlet guide vane again.The relative compressor efficiency that A is ordered is about 0.985.When under the capacity that descends because of the power demand that reduces, operating, Zong the air compression machine operation moves to the B point with the decline of foregoing relative suction volume flow and relative compression ratio along with the IGCC system.Along with the generation of further closing, the compressor operation condition moves to the C point, and finally moves to the D point, and this is a compressor minimum operation capacity, wherein compressor vanes to the greatest extent mechanically maximum possible close.Therefore, compressor efficiency is high when the maximum capacity of A point representative, is low and close the border under the part in the limit pass of C and D point representative.
The compressor operation curve of the oxygen product compressor 51 when Fig. 4 has provided operation in the gamut of flowing of on the correspond to described gas turbine engine systems operating range of Fig. 3 and compression ratio.At the design operation capacity of this system, the oxygen product compressor is at the A point operation.Along with closing increase, the oxygen compression machine operation moves to the C point from the B point successively, and finally moves to the D point when maximum is closed, and operates under the maximum volume thruput at this compressor, and wherein compressor vanes is in the maximum fluidity position.In order to make compressor in the Close All scope, have operability, compressor must gas turbine engine systems design operation capacity in low relative efficiency zone at the A point operation.
As the result of this required wide scope of design, oxygen product compressor 51 cuts out operation down in high efficiency in maximum, and operates under the normal system design capacity in poor efficiency.This is a kind of undesirable operational circumstances, because compressor will move the on-stream period (time) of suitable one section part under poor efficiency.Similar problem also is present in nitrogen product compressor 61 and 67, and it has and Fig. 3 similar operation curve.
In the part of use defined pass closed region between the A of Fig. 2 point (gas turbine capacity or full load) and B point of the gas that the present invention extracts out by restriction and only the main air compressor 43 by the gas turbine operational load under the B point offers air separation equipment with air and sets forth this undesirable operational circumstances.Relatively operating under the constant compression force in the pass closed region of air separation equipment under the B point, for example shown in 160～165 pounds of/square inch scopes in operate, and do not use the gas of extraction for the air separation equipment charging.Will be because in this operator scheme, contract all air of machine 3 by firing chamber 11 from gas turbine air pressure sky, thus heating-up temperature (firing temperature) may reduce because when closing, there is small amount of fuel 9 burned; Yet, may be higher by the mass flow rate of gas turbine 15, and the efficient of turboexpander may not be subjected to obviously to influence.
Therefore, in the present invention, between A among the figure of air separation equipment below Fig. 2 and the B point, under the pressure that reduces, under the situation that feeding air is provided by main air compressor effluent 45 and the gas 37 extracted out, operate.At B point D
*Between (maximum is closed) point, air separation equipment 39 and main air compressor 43 are operated under the pressure of substantial constant.Still operation between the A of Fig. 2 middle graph and D point of gas turbine air compressor 3, but between B and D point, the flow of the gas 37 of extraction is 0, and all pressurized air 5 will flow through firing chamber 11.The preferred minimum operational pressure of B point expression air separation equipment 39 is 160-165 pound/square inch for the example of Fig. 2.This pressure minimum needs to change with gas turbine and air separation equipment design, is generally 120～260 pounds/square inch.
In the down periods, by or be higher than under the selected minimum operational pressure and operate air separation equipment, can make the pressure of oxygen of the present invention and nitrogen product 47 and 49 be higher than the pressure of typical operation practice between B and the D point (Fig. 2).At B of the present invention, C
*With D
*Point (Fig. 2) operation period, oxygen and nitrogen product pressure and air separation feed pressure substantial constant, this and in the typical operation practice between B, C and the D operating point pressure reduce antithesis gradually.This feature of the present invention allows operation main air compressor 43 and product compressor 51,61 and 67 in very narrow compression ratio range.This makes the operating efficiency of compressor higher conversely again, just as described below.
Fig. 5 has provided the compressor operation curve that is designed to according to the main air compressor 43 of the present invention's operation.Under full design gas turbine operation capacity, compressor is at the A point operation, and simultaneously along with the generation of closing, compressor is operated (these are corresponding to point of the A among Fig. 2 and B point) between A and B point.At B, C
*With D
*Between the point, compressor is with constant head pressure and compression ratio operation.The minimal design overall compression ratio be defined as when compressor at B, C
*With D
*Compression ratio when operating between the point.The relative suction pressure of design maximum is represented by the B point.
Fig. 6 has provided the compressor operation curve that is designed to by the oxygen product compressor 51 of the present invention's operation.Under full design IGCC operation capacity, compressor is at the A point operation, and when closing when carrying out, compressor is operated (these are corresponding to A among Fig. 2 and B point) between A point and B point.At B, C
*With D
*Between the point, compressor is with constant head pressure and compression ratio operation.The total compression ratio relatively of design maximum is defined as at B, C
*With D
*Ratio when operating between the point.B point expression design maximum sucks volume flow relatively.The relative operating efficiency that A of the present invention is ordered (being present in most IGCC operating times) is about 0.99.On the contrary, the relative efficiency that corresponding A order in Fig. 4 only is about 0.85, and this A point has been described and do not used when of the present invention at the typical operation that designs under the gas turbine capacity.Therefore, the inventive method can design in narrower total compression ratio relatively and relative suction volume flow range and operate the oxygen product compressor, and this makes again that conversely the whole operation efficient of compressor is higher.
When according to common practice, in the gamut that gas turbine and air separation system are closed, adopt when bleeding, nitrogen product compressor 61 and 67 will have and the similar operating characteristics of the operating characteristics of oxygen product compressor 51 shown in Figure 4.When air separation equipment 39 was operated by the present invention, nitrogen product compressor 61 can design and operate according to the mode identical with oxygen product compressor shown in Figure 6 51 with 67.Therefore, when gas turbine engine systems is operated, can realize higher operation efficiency to all three product compressors 51,61 and 67 under design capacity according to the present invention.The definition that sucks volume flow for the nitrogen compressor 61 and total compression ratio relatively of 67 design maximum and design maximum relatively is with top identical to the given definition of oxygen product compressor 51.
The prior art method of improving the efficient of gas turbine in the IGCC system and air separation equipment has a lot, but people do not recognize, can improve total efficiency and reduce electric cost in the effect of bleeding and increasing the air separation equipment main air compressor of down periods restriction from the gas-turbine compressor to the air separation equipment.According to prior art, this is a kind of unforeseeable conclusion, because according to the present invention, in the down periods, gas turbine possible operation efficient is not high, and (gas of extraction can be drained, lower firing chamber heating-up temperature perhaps may take place), and independent air separation compressor must have bigger load.According to the present invention, the operation of air separation equipment product compressor is but so not strict; Because closing operation is determining the selection of compressor, so these compressors can be designed to more efficient full load operation.
Embodiment
The IGCC system of imitation Fig. 1, in order to the total efficiency of relatively operating according to the air separation plant of (1) existing practice, the charging that wherein enters into air separation equipment 39 is included in the gas 37 of some extraction in the whole air separation equipment operating range, with in order to relatively according to the total efficiency of (2) operation of the present invention, wherein bleed and only when the air separation equipment feed pressure that is higher than 147 pounds/square inch, just use.In this embodiment, because the variation of ambient temperature, close and be present in most situations, just the following is with see like that.Under design capacity (being similar to the A point of Fig. 3-6), average actual compression ratio is as follows: for oxygen gas-turbine compressor 3 is 13.0, is 13.0 for main air compressor 43; For oxygen compressor 51 is 10.0, and reaching for backflow nitrogen compressor 67 is 5.0.Similar with D point among Fig. 2, close or during minimal flow, average actual compression ratio is as follows: to gas-turbine compressor 3 is 9.0 in maximum; To main air compressor 43 is 9.0, is 18.0 to oxygen compressor 51, is 6.5 to backflow nitrogen compressor 67.These compression ratios are representative compression ratios of " F " technology gas turbine.Air separation equipment 39 is limited size with generation oxygen and the nitrogen required to the IGCC system, and do not flow out product oxygen or nitrogen.The IGCC system is 23,41,59,75 and 95 operations down in ambient temperature, and main air compressor 43, oxygen product compressor 51 and backflow nitrogen compressor 67 are being calculated compressor efficiency under the full load and to selected temperature under each said temperature under sub load.
Provided the result of calculation according to existing practice (bleeding to air separation equipment in whole gas turbine operating range) in the table 1, table 2 has provided the result of calculation according to the present invention's operation (only bleeding to air separation equipment when the air separation equipment feed pressure that is higher than 147 pounds/square inch).Relative compressor efficiency to last two kinds of situations and three kinds of compressors compares under 41,59 and 95 °F in full load, and the result is summarized in the table 3.As can be seen, the relative efficiency of main air compressor is in the present invention than low slightly in existing PRACTICE OF DESIGN, but the relative efficiency of oxygen and nitrogen compressor is in the present invention but than obviously high in existing PRACTICE OF DESIGN.
When ambient temperature is 41,59 and 95 °F, average in the relative efficiency under the full load for each compressor, calculate the average efficiency ratio of each compressor with these average efficiencys.This average efficiency is than the average relative efficiency of the average relative efficiency that is defined as the inventive method divided by existing practice.Be designed to situation for compressor wherein according to the existing practice of in entire I GCC operating range, bleeding to air separation equipment, calculate each total power consumption of three kinds of air separation equipment compressors, with normalization as a result to obtain the relative power consumption of every kind of compressor.Secondly, with above-mentioned definite average efficiency than calculating the relative power consumption of each compressor designed according to this invention with relative power consumption.The result provides in table 4, and these results show that when full load IGCC design capacity, the total output that air separation equipment of the present invention consumed is 3.3%, is lower than the corresponding power consumpiton according to the equipment of existing practice.
Table 1
The compressor operation data of existing practice
| Compressor (Fig. 1) | The IGCC load | Ambient temperature (°F) | Relative overall compression ratio | Suck volume flow relatively | Relative efficiency |
| Main air compressor (43) | Entirely | ????95 | ????1.000 | ????1.200 | ????96.0 |
| Entirely | ????59 | ????1.034 | ????0.919 | ????99.5 | |
| Entirely | ????41 | ????1.023 | ????0.815 | ????98.2 | |
| Entirely | ????23 | ????1.000 | ????0.805 | ????98.1 | |
| Part | ????75 | ????0.739 | ????0.814 | ????92.0 | |
| Part | ????41 | ????(1) | ????(1) | ????(1) | |
| Oxygen product compressor (51) | Entirely | ????95 | ????0.639 | ????0.850 | ????85.0 |
| Entirely | ????59 | ????0.612 | ????0.848 | ????85.0 | |
| Entirely | ????41 | ????0.621 | ????0.862 | ????85.0 | |
| Entirely | ????23 | ????0.639 | ????0.846 | ????85.0 | |
| Part | ????75 | ????0.942 | ????1.006 | ????99.5 | |
| Part | ????41 | ????1.100 | ????1.100 | ????99.0 | |
| Nitrogen product compressor (67) | Entirely | ????95 | ????0.819 | ????0.839 | ????95.0 |
| Entirely | ????59 | ????0.801 | ????0.837 | ????95.0 | |
| Entirely | ????41 | ????0.807 | ????0.851 | ????95.0 | |
| Entirely | ????23 | ????0.819 | ????0.835 | ????95.0 | |
| Part | ????75 | ????1.007 | ????1.002 | ????100.0 | |
| Part | ????41 | ????1.100 | ????1.100 | ????99.0 |
(1) main air compressor is closed, and all air raw materials derive from gas turbine
Table 2
Compressor operation data of the present invention
| Compressor (Fig. 1) | The IGCC load | Ambient temperature (°F) | Relative overall compression ratio | Suck volume flow relatively | Relative efficiency |
| Main air compressor (43) | Entirely | ????95 | ????1.000 | ????1.200 | ????96.0 |
| Entirely | ????59 | ????0.944 | ????0.883 | ????99.0 | |
| Entirely | ????41 | ????0.903 | ????0.790 | ????97.0 | |
| Entirely | ????75 | ????1.000 | ????1.202 | ????96.0 | |
| Part | ????41 | ????0.754 | ????0.631 | ????85.0 | |
| Oxygen product compressor (51) | Entirely | ????95 | ????0.794 | ????0.844 | ????95.0 |
| Entirely | ????59 | ????0.876 | ????0.953 | ????96.0 | |
| Entirely | ????41 | ????0.920 | ????1.010 | ????99.4 | |
| Entirely | ????75 | ????0.810 | ????0.872 | ????97.0 | |
| Part | ????41 | ????1.100 | ????1.100 | ????99.0 | |
| Nitrogen product compressor (67) | Entirely | ????95 | ????0.949 | ????0.845 | ????96.0 |
| Entirely | ????59 | ????1.008 | ????0.954 | ????99.7 | |
| Entirely | ????41 | ????1.056 | ????1.010 | ????99.6 | |
| Entirely | ????75 | ????0.949 | ????0.872 | ????97.0 | |
| Part | ????41 | ????1.100 | ????1.100 | ????97.0 |
Table 3
The relative total power consumption of equipment blows off when the IGCC full load
| Compressor (Fig. 1) | Total output has now and puts into practice (%) relatively | The average efficiency ratio | Relative total output, the present invention (%) |
| Main air compressor (43) | ????37.6 | ????1.006 | ????37.8 |
| Oxygen product compressor (51) | ????15.6 | ????0.878 | ????13.7 |
| Nitrogen product compressor (67) | ????46.8 | ????0.966 | ????45.2 |
| Sum | ????100 | ????96.7 |
Relative total output=relative total output * average efficiency ratio
(the present invention) (existing put into practice) is as from the relative efficiency of table 1 as can be seen, total power consumption is at sub load condition end height when adopting the inventive method, but because sub load is present in small part in the time, so the efficient that full load experienced in most of times is higher.
In the above-described embodiments, the IGCC system with the present invention's operation compares air separation power decline 3.3% under the full load condition with existing practice.Consume the 400MW power station of 50MW for air separation equipment wherein, it 3.3% be 1.65MW that air separation plant power descends, and this is equivalent to annual saving $723,000 during for $0.05/KWH at cost of energy.
Therefore, and compare, the invention enables the air separation equipment of IGCC power generation systems to operate in more effective mode by existing practice.Because the air separation equipment compressor design becomes in narrower compression ratio range operation, mainly be because when the IGCC system operated under full design load, oxygen and nitrogen product compressor were with high efficiency manipulation so realize more effective total operation.When the product compressor must be designed to operate in wide compression ratio model, i.e. situation when gas that in entire I GCC operating range, utilize to extract out, when the IGCC system operated under full load, these compressors were with obviously lower efficient operation.In addition, by continuous running air separation equipment in the four corner of IGCC load, can avoid with the starting of the main air compressor of air separation equipment and close relevant poor efficiency.
Fundamental characteristics of the present invention has fully been described in the disclosure in front.One of ordinary skill in the art will appreciate that the present invention, and make various improvement, and do not depart from essence spirit essence of the present invention, with scope that does not depart from appended claims and jljl mutually.
Claims (13)
1. the method for an operation associating gas turbine/air separation system under sub load, this method is included in pressurized air in the gas turbine air compressor, at least a portion gained pressurized air and fuel are burnt in gas-turbine combustion chamber, to form hot combustion products, this hot combustion products expands in the gas turbine quencher, described quencher Driven Compressor and the optional generator that drives, air is separated into rich nitrogen and oxygen enriched product in low temp air fractionation system, wherein, the feeding air that enters into air separation equipment is provided by main air compressor, and optional provide by extention pressurized air from the gas turbine air compressor, wherein unite gas turbine/air separation system with the sub load operation, so that:
(a) when the gas turbine air compressor provides pressurized air with the given operation pressure greater than minimum air separation equipment feed pressure, air separation equipment with the essentially identical feed pressure operation of given operation pressure, and feeding air by main air compressor be provided to air separation equipment from the extention pressurized air of combustion gas turbine air compressor; Or
(b) when the gas turbine air compressor to be substantially equal to or when providing pressurized air less than the given operation pressure of minimum air separation equipment feed pressure, air separation equipment is operated with the feed pressure that is substantially equal to minimum air separation equipment feed pressure, and the feeding air that is fed in the air separation equipment is provided by main air compressor, does not have the additional compressed air from the gas turbine air compressor.
2. according to the process of claim 1 wherein that minimum air separation equipment feed pressure is 80～500 pounds/square inch.
3. according to the process of claim 1 wherein main air compressor with one of two kinds of patterns operations, so that
(a) when main air compressor with greater than the operation of the head pressure of minimum air separation equipment feed pressure the time, main air compressor with greater than the total compression ratio relatively of its minimal design be lower than the relative volume flow that sucks of its design maximum and operate; Or
(b) when main air compressor being substantially equal to head pressure when operation of minimum air separation equipment feed pressure, main air compressor basically with the total compression ratio relatively of its minimal design with or be lower than the relative volume flow that sucks of its design maximum and operate;
Wherein the relative volume flow that sucks with design maximum of the total compression ratio relatively of the minimal design of main air compressor mainly produces when minimum air separation equipment feed pressure.
4. according to the method for claim 3, wherein main air compressor is operation under 80～600 pounds/square inch in head pressure.
5. according to the method for claim 1, this method further comprises to be compressed oxygen enriched product in oxygen compressor, and this compressor is with any operation in two kinds of patterns, so that:
(a) when main air compressor is operated under the head pressure greater than minimum air separation equipment feed pressure, oxygen compressor is being lower than the total compression ratio relatively of its design maximum and is being lower than relative the suction under the volume flow of its design maximum and operates; Or
(b) when main air compressor basically with head pressure that minimum air separation equipment feed pressure equates under when operating, oxygen compressor basically the total compression ratio relatively of its design maximum with or be lower than relative the suction under the volume flow of its design maximum and operate;
Wherein the total compression ratio relatively of the design maximum of oxygen compressor relative with design maximum suck volume flow occur in main air compressor basically with head pressure that minimum air separation equipment feed pressure equates under in the situation of operating.
6. according to the method for claim 5, wherein oxygen compressor is operation under 120～2000 pounds/square inch in head pressure.
7. according to the method for claim 5, this method further comprises by using the compressed oxygen enriched product vaporized carbon raw material from air separation equipment to produce the fuel that is used for gas-turbine combustion chamber.
8. according to the method for claim 7, this method further comprises the rich nitrogen product of near small part to be compressed in nitrogen compressor, to be used for the technology of vaporized carbon raw material.
9. method according to Claim 8, wherein this nitrogen compressor is with any operation of two kinds of patterns, so that:
(a) when main air compressor is operated under the head pressure greater than minimum air separation equipment feed pressure, nitrogen compressor is being lower than the total compression ratio relatively of its design maximum and is being lower than relative the suction under the volume flow of its design maximum and operates; Or
(b) when main air compressor basically with head pressure that minimum air separation equipment feed pressure equates under when operating, nitrogen compressor basically the total compression ratio relatively of its design maximum with or be lower than relative the suction under the volume flow of its design maximum and operate;
Wherein the total compression ratio relatively of the design maximum of nitrogen compressor relative with design maximum suck volume flow occur in main air compressor basically with head pressure that minimum air separation equipment feed pressure equates under in the situation when operating.
10. according to the method for claim 9, wherein nitrogen compressor is operation under 50～2000 pounds/square inch in head pressure.
11. according to the method for claim 1, this method further comprises the rich nitrogen product of near small part to be compressed in nitrogen compressor, and the compressed nitrogen of gained is incorporated in the gas-turbine combustion chamber.
12. according to the method for claim 11, wherein nitrogen compressor is with any operation of two kinds of patterns, so that:
(a) when main air compressor is operated under the head pressure greater than minimum air separation equipment feed pressure, nitrogen compressor is being lower than the total compression ratio relatively of its design maximum and is being lower than relative the suction under the volume flow of its design maximum and operates; Or
(b) when main air compressor basically with head pressure that minimum air separation equipment feed pressure equates under when operating, nitrogen compressor basically the total compression ratio relatively of its design maximum with or be lower than relative the suction under the volume flow of its design maximum and operate;
Wherein the total compression ratio relatively of the design maximum of nitrogen compressor and design maximum suck volume flow relatively and occur in the situation that main air compressor operates under identical with minimum air separation equipment feed pressure basically head pressure.
13. according to the method for claim 12, wherein nitrogen compressor is operation under 120～2000 pounds/square inch in head pressure.
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| CN 96112071 CN1155619A (en) | 1995-11-07 | 1996-11-04 | Operation of integrated gasification combined cycle power generation systems at part load |
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| CN 96112071 CN1155619A (en) | 1995-11-07 | 1996-11-04 | Operation of integrated gasification combined cycle power generation systems at part load |
| US553187 | 2000-04-20 |
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