EP3353387A1 - Procédés et modes de réalisation de technologie de composition d'enthalpie et leurs machines - Google Patents

Procédés et modes de réalisation de technologie de composition d'enthalpie et leurs machines

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Publication number
EP3353387A1
EP3353387A1 EP15841686.7A EP15841686A EP3353387A1 EP 3353387 A1 EP3353387 A1 EP 3353387A1 EP 15841686 A EP15841686 A EP 15841686A EP 3353387 A1 EP3353387 A1 EP 3353387A1
Authority
EP
European Patent Office
Prior art keywords
turbine
heat
working fluid
pressure stage
evaporators
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.)
Withdrawn
Application number
EP15841686.7A
Other languages
German (de)
English (en)
Inventor
Arne Jonsson
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ect Power AB
Original Assignee
Ect Power AB
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Filing date
Publication date
Application filed by Ect Power AB filed Critical Ect Power AB
Publication of EP3353387A1 publication Critical patent/EP3353387A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K7/00—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating
    • F01K7/16—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type
    • F01K7/18—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type the turbine being of multiple-inlet-pressure type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/06—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using mixtures of different fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours

Definitions

  • the invention relates to an apparatus of Organic Rankine Cycle type including a closed loop working fluid circuit operable between a heat source and a heat sink. More specifically the invention relates to ORC apparatuses having a working fluid circuit including: a heat exchanger arrangement for vaporizing and/or superheating a working fluid by exchanging energy from the heat source; at least one turbine for expanding the vaporized/superheated working fluid; condensing means connectable to the heat sink for condensing the expanded working fluid from the turbine; and pumping means for pumping and pressurizing the condensed working fluid to the heat exchanger arrangement.
  • ORC apparatuses having a working fluid circuit including: a heat exchanger arrangement for vaporizing and/or superheating a working fluid by exchanging energy from the heat source; at least one turbine for expanding the vaporized/superheated working fluid; condensing means connectable to the heat sink for condensing the expanded working fluid from the turbine; and pumping means for pumping and pressurizing the condensed working fluid to the heat
  • the invention relates to an improved ORC of the type initially mentioned, in which the heat exchanger arrangement comprises at least three parallel coupled evaporators forming at least three pressure stages on the working fluid side, and providing one outlet per pressure stage for connecting to the at least one turbine.
  • the at least one turbine is a single turbine including one inlet per pressure stage. Each inlet connected to respective pressure stage outlet. The turbine further having a common outlet for the expanded working fluid.
  • the turbine may e.g. drive a propeller axis, a compressor or a pump.
  • the heat exchanger arrangement includes three evaporators, one for a low pressure stage, one for a medium pressure stage, and one for a high pressure stage, at least one economizer per pressure stage, and optionally at least one superheater per pressure stage.
  • the heat exchanger arrangement includes: one economizer at the low pressure stage, two economizers at the medium pressure stage, and three economizers at the high pressure stage.
  • the economizers at respective pressure stage being serial connected (if more than one) on the working fluid side.
  • the heat exchanger arrangement is configured to heat the working fluid at each pressure stage to an individual temperature starting point at the corresponding turbine inlet, each starting point selected to be in the dry/superheated region.
  • the heat exchanger arrangement is configured such that each starting point is selected to provide the turbine expansion to end in within +_5 °C of a common temperature and pressure end point in the dry/superheated region.
  • the common end point is preferably situated about 5-10 % of the latent heat/enthalpy in the dry/superheated region of the saturation curve from the saturation curve. More preferably, the common end point is situated about 1-2 % of the latent heat/enthalpy in the dry/superheated region of the saturation curve from the saturation curve.
  • At least two of the evaporators are coupled in series on the heat source side, such that at least a portion of the heat source flow is directed through the evaporators in series. More, preferably at least three evaporators are coupled in series on the heat source side.
  • the pressure stages are selected such that the vaporization temperatures of the evaporators are within T2+ A n *(Tl-T2) +-15 %, where
  • An (l/(n+l), 2/(n+l),...,(n)/(n+l)), where n being the number of evaporators, and where Tl being the temperature of the heat source and T2 the temperature of the heat sink.
  • the variation is selected as +-10%.
  • the turbine is of a turbo machine type, e.g. an impulse/action type or a reaction turbine and having at least two inlets, and directing means in the form of guiding vanes and/or nozzles for directing a flow from said inlets on to different radii of one common turbine wheel of the turbine.
  • the turbine may be a reaction turbine preferably of a radial or a mixed flow type with a centripetal (inwards) flow direction with a casing and at least one runner/wheel with working blades, at least two inlets and one common outlet where the inlets in turn are connectable to guiding vanes/nozzles in the turbine casing for expansion of the gas at different radii.
  • the turbine may alternatively be an impulse/action type with a disc that has blades at different radii to match the driving expanded flow from the nozzles whereby at least two sets of the nozzles are situated at different radii and the remaining at equal radii but at separate angular sectors.
  • the turbine/expander may be of a positive displacement machine type with several stages by having displacement volumes determined by a first actual flow stream of the working fluid to which part working fluid streams are further added between the stages and that the downstream displacement sizes are correspondingly increased to swallow the total vapor flows.
  • displacement machine is a screw expander/turbine with one or several screws designed to be a 2 or 3 stage machine with intermediate inlets for said part flow streams between the stages and that the downstream screw displacement/volume capacity is designed by selecting shape, size and/or the number of the "pistons" in a first/male and slots in a second/female rotor cooperating with the first to swallow both the actual and the total volume flows.
  • Fig. 1 Shows waste heat power process circuits of prior art.
  • Fig. 2 shows the temperature profile with T as temperature and JF as heat flow.
  • Fig. 3a and 3b shows the temperature profile for the heat source when heat is removed at a high and a low temperature range respectively.
  • Fig. 4 Individual temperature profiles Fig. 5 The temperature profile - temperature (y-axis) / heat flow (x-axis) curves Fig. 6 Circuits for the working fluid.
  • FIG. 8 Heat source circuit.
  • Figures " 13H”, “13M” and “13L” mark the different vaporization stages.
  • Fig. 11 Section of an axial turbine wheel (left) and inlet vanes/nozzles (right).
  • Fig. 12 Section of a radial turbine for three different admission data. Circuits in the volutes 61 and 62 are obtained by dividing the peripheral circumference in two parts.
  • a waste heat process using sensible heat has normally three different circuits; a heat source circuit 1, a working fluid circuit 2 and a heat sink 3, Fig. 1.
  • the fluid of the heat source (gas or liquid) passes and exchanges heat, in a possible superheater 14, an evaporator 13 and an economizer 12 with a decrease in temperature from ⁇ to 1".
  • the working fluid in 2 passes said heat exchangers with a change in state from liquid to vapor with a corresponding increase of its energy content from 2 to 2".
  • the heat sink 3 cools the condenser and may have a pump 17.
  • the heat sink may e.g. be ambient (cold) water or air or indirectly a liquid from a cooling tower or an air-cooled radiator.
  • FIG. 2 A graph, Fig. 2, with heat flow Was abscissa (x-axis) and temperature Jas ordinate (y- axis) gives an excellent view of all important data.
  • the heat source 1 is given by an approximately straight line, the working process 2 by a closed circuit 2 and the heat sink by the line 3.
  • the said components are marked with equal figures as in Fig. 1.
  • the evaporation is shown as the line 13, the economizer by 12 and the superheater by 14.
  • the line 13 is shown oblique to the W-axis that means the liquid vaporizes at varying temperatures or at non-isothermal conditions (as in the Kalina process). This is typical for mixtures of different media.
  • the line 13 is horizontal as it vaporizes at a constant temperature. Similar conditions are valid for the line 16 at the condenser.
  • An expansion of the working fluid is marked 15 and 151 of which 15 represents the useful mechanical work obtainable as input/output to/from the turbine.
  • the size of this work is also given as the distance 0-150 while the total source heat flow is 0-1".
  • the temperature profile as shown in fig. 2 is split in two parts an outer or gross part defined from the heat source 1 and heat sink 3 with a maximal temperature difference from the points ⁇ and 1" with temperatures Tj and
  • thermo differences are required to drive a heat transfer.
  • these differences are marked 12', 12", 13", 14" and 16'.
  • the size of the heat exchanger areas depends on the max and the min difference.
  • An optimal area sizing can now be based on the said gross efficiency and the said temperature differences from the temperature profile.
  • a temperature heat flow part marked as 151 is the waste heat from the inner process 2. As the temperature is above that of the heat sink it can, known per se, be recovered by a recuperator and utilized for an improvement of the inner process shown in fig 2 as 152, parallel moved to the right as a tail for increasing the heat source.
  • US 8,438,849 B2 has two heat sources with different temperatures/pressures, where in two alternatives vapor from a high pressure turbine in series with vapor from the other sources is fed to a low pressure turbine.
  • the two heat sources are coupled in parallel to independent vaporizers and independent turbines and then to a common condenser.
  • the two heat sources have independent circuits including turbines and condensers with water as working fluid for one of the circuits.
  • US 8,474,262 B2 has one heat source and two separated independent circuits complete with all components as well as turbines, where the split between the two circuits is optimized.
  • US 2010/0071368 Al has an ORC with a cascade coupling where expanded vapor from the high pressure turbine is fed to the low pressure turbine and in an alternative parallel circuits each coupled to a turbine. In a further alternative there are two totally independent circuits of which one has water as working fluid.
  • US 2010/0242476 Al this is similar to US 6,857,268 B2 with a cascade solution for high and low pressures circuits.
  • US 2010/0242479 Al similar to US 2010/0242476 Al, but with a back end for generation of heating/refrigeration added.
  • the screw expanders can have wet condition for the working fluid, which normally is avoided due to damage risk in normal turbines.
  • US 2014/0033711A1 has evaporation at different pressures/temperatures each coupled to two expanders/turbines of the screw type for wet service.
  • WO 2014/0211708 has several heat sources connected to separate evaporators, turbines in parallel for the heat source fluid as well as the working fluid.
  • the circuits are connected to one common condenser.
  • the present invention ECT uses in contrast to the prior art a single heat source and multiple vaporization temperature/pressures.
  • the flow pattern through the heat exchangers (evaporators) is parallel for the working fluid, that not is common, and series for the heat source fluid. The reason is to gain more electric output from the same heat source by matching the temperature profile of the heat source fluid with that for the working fluid. The tail of the heat source profile will then get a low outlet temperature close to that of the heat sink.
  • WO 2013/171685 Al shows a "multistage" radial turbine design for adding/removal of a part fluid flow (intermediate superheating) with a pressure between the pressures and with adding/removal also between the normal in- and outlets.
  • the main flow direction is centrifugal (outwards).
  • the turbine design is similar to a Ljungstrom radial turbine but with one of the counter rotating part replaced by a stationary vane set.
  • DE 10 2012 021 357 Al 2014.05.08 shows an ORC with evaporation in two stages with heat taken from the heat source and then in a further stage with heat from a recuperator. The main vapor streams and part streams are fed into a multistage axial turbine between the turbine stages.
  • CN 103195519 A shows an ORC with 4 evaporation stages coupled in series and driven by heat from the heat source and a further stage driven by heat from a recuperator. Vapor from the working fluid is schematically supplied to different parts of a turbine. If the working circuits are coupled in series as in this prior art separating means must be arranged between the stages as a pressure difference between liquid out from a preheater and into an evaporator due to obtain sufficient NPSH for avoiding cavitation in the pumps. Alternatively the separation could be done by a vapor/liquid tank/boiler or the pumps placed well below the exchangers. Another disadvantage is that separate pumps are necessary
  • ECT is an acronym for "Enthalpy Compounding Technology”.
  • ECT is an invention with the intention to improve the economic conditions for generating electricity out from waste heat sources. Typical for these are that the heat is found in a sensible form that means that the temperature is gradually decreasing when heat is taken out.
  • the ECT may take advantage of the temperature profile for a sensible heat source in that a performance optimum is selected.
  • the performance optimum for a process with one single evaporation process below a temperature difference below 100 °C is an average vaporization temperature (e.g. a vertical mean of line 13 in fig.2)) of about T2+1/2 *(T2-T1) with a variation of not more than +- 15 %.
  • Tl being the temperature of the heat source and T2 the temperature of the heat sink.
  • the total or gross efficiency/gain is first and foremost defined as the net output as mechanical work in relation to the available heat between the heat source max temperature down to the minimum temperature of the heat sink.
  • a part efficiency is sometimes erroneously calculated for the working circuit itself that, however, cannot be used for any technical and/or economical consideration.
  • the fig. 3a and Fig.3 b shows the temperature profiles, when heat is removed from the heat source fluid.
  • Fig. 3a shows, when heat is removed in a high temperature range and 3b ditto in a low temperature range.
  • the removed heat may be used for e.g. some chemical process or for the low range for district heating.
  • the optimal value will now coincides with a gravity center for the line from 1 ' , Ch to 1 " .
  • Table 1 An example with big differences in total efficiency in dependence of the evaporation temperature for cases, where the heat source is 90 °C and the heat sink is
  • the ECT process may feature several different vaporization temperatures or pressure levels at which heat is transferred in the process, preferably as separate part flow circuits 2H, 2M and 2L, fig. 4, all may have about equal
  • T is the temperature and W is the heat flow.
  • All the vaporization temperatures are then optimized for max output/gain.
  • a pure or an aezotrophic fluid is used with 3 different vaporization temperatures.
  • at least one of the pressure level may be above the critical point (critical pressure) for the working fluid, a point above which no vaporization occurs at heating.
  • One embodiment of the invention uses basically evaporation with at least 3 different temperatures/pressures, usually 3, at at least one heat source at a certain given max temperature.
  • a relative temperature Treiative is placed on the y-axis and a relative heat Wreiative on the x-axis.
  • the dotted line is the heat source 1 and the solid stair-shaped line represents the working fluid.
  • the horizontal plateaus are the vaporization at the constant temperatures 2H, 2M and 2L respectively. These temperatures are optimized for highest efficiency/gain.
  • the shown stair-shaped line gives a very good heat source utilization. However, several/infinite, infinitely small stair steps create the best possible process.
  • the differences at the knees (pinch points), 12" are further economically optimized with regard to obtained electrical output/gain and the cost of the heat exchangers.
  • the differences at 12" are the driving "force" for the heat transfer. Typical is here differences less than 5 % of the temperature span to 1" and with preferable values of 2-3 %.
  • the relative temperature on the waste heat in the own process then is 0.18 of the relative temperature span 1 to 0. Compared to the present conventional methods more than a doubled gain as electricity is obtained at a given and equal source of waste heat.
  • n being the number of evaporators
  • Tl being the temperature of the heat source and T2 the temperature of the heat sink.
  • the tolerance being +- 10%.
  • the vaporization temperatures could be selected as (40°C, 60 °C, 80 °C), the values with variation of +- 15%, preferably +-10%.
  • each heat exchanger has four connection ports for in/out for the two fluids exchanging heat, compare figure 1.
  • the figures 6-8 show the exchanger coupling for each of the fluids, one at the time.
  • Fig.6, 7, and 13 show alternative couplings, of the heat exchanger arrangement 12-14, on the working fluid side.
  • ECT has according to the invention the part circuits for the working fluid high H, medium M and low L pressures in fig. 6 coupled in parallel.
  • the heat exchanger arrangement 12- 14 comprising at least three parallel coupled evaporators forming at least three pressure stages (L, M, H) on the working fluid side.
  • Each pressure stage connects to the turbine 15 which is designed to receive and expand vapor from each pressure stage.
  • Pumps 11 pressurizes each pressure stage (L, M, H).
  • the heat exchanger types 12, 13 and 14 are equal to the prior art in fig. 1.
  • the total solution has optimized sizing of the part flows in the circuits.
  • the part flows are roughly one third in each.
  • the pumps 11 raises the pressure from COO to L0, M0, and HO for respectively pressure stage L, M, and H.
  • the economizers 12L, 12M, 12H preheats the working fluid to LI, Ml, and HI to respective evaporator 13L, 13M, and 13H.
  • the evaporators 13L, 13M, 13H vaporizes the working fluid to L2, M2, and H2 to respective superheater 14L, 14M, and 14H.
  • the superheaters 14L, 14M, and 14H superheats the working fluid to S I, S2, and S3.
  • the superheated working fluid is then expanded to the common end point CI 23.
  • the heat source flow circuit, fig. 8, starting at and ending at 1" has a main heat flow path given by the three evaporators 13H, 13M and 13L together with minor flows for the other components.
  • the evaporators 13H, 13M and 13L are coupled in series. The reasons are to make it possible to use a maximum of heat from the heat source and simultaneously achieve small/optimal values for the pinch points at the knees, compare fig. 5.
  • the basic preheaters/economizers 12H and 12M in fig.8 are divided in several 12M, 12M' and 12H, 12H' and 12H" with connection to the heat source circuit between 13M-13L and between 13M-13L and 13H-13L respectively.
  • the said preheaters/economizers are then heated from the heat source and its temperatures with lowest possible consumption of heat/temperature. The gain will then be more heat/temperature capacity for the downstream evaporators 13M and 13L respectively and in turn better overall heat performance.
  • Fig.14 further shows an alternative couplings on the heat source side of the heat exchanger arrangement 12-14 corresponding to the working fluid connection of fig 13.
  • the heat exchanger arrangement of the working fluid circuits have three of the evaporators coupled in parallel, while the heat source circuits have three of them coupled in series.
  • ECT Due to cost reduction ECT uses preferably a very small superheating of the vapor from the part evaporators normally with different values for all of them.
  • Fig. 9 describes a pressure p enthalpy h graph. Shown is also isotherms in °C, isenthrops (Isen) and steam/vapor quality x.
  • the superheatings to points S I, S2 and S3 for the circuits high 2H, medium 2M and low 2L respectively, are according to the invention selected so that during and after expansion in a turbine to expanded and superheated vapor to one about common point C I 23.
  • recuperator When the working fluid has a lower slope on its saturation curve than the isenthrops corrected for turbine losses a recuperator may be used. By the common point C 123, exergy losses are avoided as when fluids with different temperatures (enthalpies) are mixed.
  • the point C123 is selected close to the saturation curve at the condensation temperature t2.
  • the horizontal distance C I 23 -CO is then according to the invention preferably selected to 1- 2 % of the latent enthalpy and no more than 5- 10 %.
  • the said superheating may be made directly in the evaporators and separately superheaters are not necessary.
  • the endpoint from the vapor expansion C123 is so adjacent to the saturation curve that heat recovery (C123 to CO) in a recuperator not is necessary.
  • the graph fig. 9 is typical for most refrigerants. Water and ammonia are diverging where a superheating must be done to avoid moisture in the turbine. However, in US 2014/0026574 Al the entire refrigerant vapor expansion is made in the moisture region CO-COO (to the left of the saturation curve). The reason is believed to be, to get condensate as a sealing liquid in an expander (turbine) of the screw type that in turn allows lower shaft speed of the expander.
  • the multistage evaporations in ECT give different enthalpies for a turbine/expander.
  • Efficiency for axial turbines as well as reaction turbines is basically related to a relation between a vapor/steam velocity c and a peripheral velocity u with a typical dependence as shown in fig. 10a.
  • the curve has here an accentuated peak.
  • efficiency is expressed versus a relation depending on enthalpy as the inverted value of u/c squared (1 / (u/c) 2 ) , fig 10 b, the corresponding curve is rather flat. This will ease the design of a turbine not only at the rated performance but also for variation in performance and for service at off design conditions.
  • the new action turbine of the impulse type, Fig. 11, has its design preferably with three sets of nozzles 65, 66 and 67 respectively designed for their actual enthalpy drops.
  • a turbine wheel 52 with centerline 53 can have about conventional blades 51.
  • the nozzles are placed radially considering the velocity ratio u/c. The flow through the turbine blades will then be close to optimum.
  • a separate blade passage may be placed at a smaller radius in the disc.
  • ORC Organic Rankine Cycle
  • the three nozzle groups may be arranged at an equal wheel radius.
  • An ECT radial/mixed flow turbine has a rotatable runner 50 with blades 51 connected by a hub 52 to a shaft with a centerline 53.
  • the runner has preferably a stepped outside diameter with the diameters D2 and D2' respectively.
  • a radially extended part between said diameters may have a separation wall 54.
  • the shaft with bearings carries the overhung runner and shaft seals built in a conventional way.
  • Said runner is operable in a casing 56 with volute shaped parties a first 61, a second 62 and a third 63 placed at at least on another part of the circumference. They are connected to different inlets (not shown) from the ECT working fluid (process) circuits.
  • a holder 64 equipped with guiding vanes sets a first one 65, a second one 66 and a third 67 are clamped by a cover 57 connected to the casing by screws 58.
  • Said cover has an outlet opening with a connection flange 59.
  • the runner blades and the said cover has a relatively tight clearance as well as the radially extended distance between the runner wall 54 and the vane holder 64 in order to avoid mitigation of the turbine performance.
  • the rotatable separation wall 54 may be replaced by said holder 64 extended radially inwards to meet the diameter D2' and having a tight axial clearance to the blades 51.
  • the at least two ECT process circuits have different enthalpy drops that in turn at an expansion give different absolute velocities c.
  • a velocity ratio u/c should equal about one to obtain a high efficiency.
  • the desired velocity ratio u/c is obtained by varying either u or c or even both of them simultaneously.
  • the flow follows a free vortex law that has the feature; that radius times the tangential component of the absolute velocity c u is constant. A smaller radius in the gap then gives a higher velocity c u .
  • the velocity c is about equal to c u .
  • the desired ratio u/c is obtained by selecting the diameters D2, D2' and/or D4, D4' accordingly.
  • the general configuration may be varied in several ways known per se.
  • the semi open runner in fig.13a may be almost fully open with a tight clearance to the casing and cover on both sides or closed with a rotatably runner cover connected to the blades.
  • This runner cover may have a sealing part to the casing cover.
  • a similar sealing could be arranged on the opposite runner side.
  • the casing as shown is radially split with access on the outlet connection side 59. Access could also be arranged on the opposite side.
  • the radially split casing could also be replaced by a casing axially split through the centerline 53.
  • the velocity ratios u/c are different for an axial impulse turbine (de Laval action type with 0 % reaction) with u/c about 0.4-0.5 and a radial turbine with 50 % reaction where u/c is equal to about one.
  • a radial turbine with 50 % reaction c is about 70 % of the value of c for an action turbine.
  • the different radii may be arranged as a stepped outside wheel diameter with 3 steps (the figure 12 shows two diameter steps).
  • the radii nozzle bank may have their outlets on different radii with a different radial gap to the turbine disc. In this gap then we get a free vortex gap that is designed to fit the entrance flow to the wheel.
  • the basic principle of the ECT can be applied on other expander/turbine types as on the broad family of positive displacement machines.
  • a triple (3 stages/cylinders in series) compound steam/vapor machine shall be mentioned.
  • the adoption to ECT means that part working fluid streams are added between the stages and the cylinder sizes are adapted to the corresponding increased vapor flows.
  • the screw expander with 2 screws, developed from the Lysholm screw compressor, or a single screw expander with side mounted sealing wheels can also be designed as a 2 or 3 stage machine with intermediate inlets for adding part flow streams between the stages.
  • the screw volume capacity is changed by selecting the size and/or the number of the "pistons" in the male and the slots in the female rotor/rotors according to the volume flow. Note, when these changes are arranged within common rotors, the screw pitch must be equal for all parts.
  • ECT By ECT the electric output/gain is more than doubled compared to conventional commercial ORC processes using the same heat source and the same heat sink. ECT compares also well with non-isothermal vaporization processes. In addition ECT has a simpler structure and better conditions for the turbine/expander.
  • the ECT improvement is based on a systematic thermodynamic al analysis, first defining a theoretical process analogous with the Carnot process working between two constant temperatures and then applying the result to practical conditions regarding working fluid and process components.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

L'invention concerne des procédés d'amélioration de la quantité d'électricité obtenue à partir de préférence de la chaleur perdue par un processus de Rankine à fluide organique (ORC) ou normal avec vaporisation à plusieurs étages, normalement trois. La chaleur perdue en forme sensible est échangée dans au moins deux évaporateurs couplés en série vers un fluide de travail de réception (par exemple un fluide frigorigène) qui passe par au moins deux de ces évaporateurs, mais couplé en parallèle. Environ 80 % de la chaleur perdue entre la température de la source de chaleur et celle du dissipateur thermique peut être utilisée pour une la production d'électricité directe. Un mode de réalisation de l'invention utilise une turbine radiale dotée d'une direction d'écoulement centripète (vers l'intérieur). Les différentes enthalpies de vapeur à partir desdits étages de vaporisation entrent dans une roue de turbine/roue (51) aux diamètres extérieurs différents (D2, D2') et/ou avec des vitesses tangentielles appropriées obtenues par différents ensembles d'aubes directrices (65, 66 et 67).
EP15841686.7A 2014-09-19 2015-09-21 Procédés et modes de réalisation de technologie de composition d'enthalpie et leurs machines Withdrawn EP3353387A1 (fr)

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CN110821707A (zh) * 2019-11-25 2020-02-21 天津大学 基于二氧化碳动力循环的柴油机余热利用梯级耦合系统
CN111042885A (zh) * 2019-12-25 2020-04-21 中国船舶重工集团公司第七一一研究所 一种回收不同温位余热的发电系统及发电方法
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FR1108442A (fr) * 1954-07-08 1956-01-12 Alsthom Cgee Perfectionnement améliorant l'utilisation des chaudières de récupération combinées à des accumulateurs de chaleur
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CN101806232A (zh) * 2010-03-17 2010-08-18 昆明理工大学 多级蒸发有机朗肯循环余热回收发电系统及其方法
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