SYSTEM FOR DETERMINING PROCESS PARAMETERS RELATING TO THERMAL PROCESSES SUCH AS, FOR INSTANCE, WASTE INCINERATION

Abstract: The invention relates to a system for thermal combustion processes of matter such as, for instance, waste incineration. The system comprises a computer for measuring parameters of the combustion of the matter, wherein, in use, matter, such as for instance waste, is supplied to the system and combusted, thereby forming a flue gas. The system further comprises means for determining the concentration of CO2, O2 and H2O in the flue gas. The computer is arranged for determining, on the basis of the measured concentrations, the rate of combustion and/or the composition of the combustible part CHyOz of the waste supplied to the system, for the purpose of process control.

Description: Title: System for determining process parameters relating to thermal processes such as, for instance, waste incineration. This invention relates to a system for determining process parameters relating to thermal combustion processes of matter such as, for instance, waste in an incinerator, comprising sensor means and a computer coupled thereto for determining the parameters, wherein, in use, matter having a combustible part CH y O 2 is supplied to the incinerator and combusted, thereby forming a flue gas. Operational management of the existing plants for waste incineration is rendered more difficult by the varying composition of the waste that is supplied to an incinerator of the plant. Due to the circumstance that changes in the properties of the waste are not recognized timely in the process behavior, the existing control systems are not properly able to regulate the process. If, however, the waste composition of the waste in the incinerator could be derived on-line, this would enable better adjustment to variations in the waste composition, thereby rendering the waste incineration process better controllable. Such a derivation, however, is highly complicated. The object of the invention is to provide a system that can be utilized in a plant for combustion of matter to meet the drawbacks outlined. Accordingly, the system for determining process parameters relating to the thermal combustion of matter is characterized in that the sensor means are arranged for measuring the fractions Xco2, X02 and XH20 in the flue gas and that the computer is arranged for determining, on the basis of the measured fractions, the composition (y/z) and/or the heat of combustion (HcHyθz,[J kg]) of the combustible part CH y O z , with X02, XH20, XCO2 respectively representing the fractions of O 2 , H2O and CO2 in the flue gas. By measuring, in accordance with the invention, just the fractions Xco2, X02 and XH20 in the flue gas, relevant parameters (the heat of combustion and/or the composition of the combustible part) for possible regulation of the matter combustion can be determined. More particularly, it holds that, in use, the computer calculates the value of Z on the basis of the formulae: wherein Xo 2 , a i r (the oxygen fraction in air supplied to the incinerator), XN2,a-r (the nitrogen fraction in air supplied to the incinerator), Xc (the uncombusted fraction of carbon) and y are predetermined values. Preferably, it will then hold that the predetermined value of Xc is inbetween 0.9 and 1. Further, it holds in particular that, in use, the computer calculates the value of HcHyOz on the basis of the formulae According to a further advanced embodiment of the system, it holds that the system further comprises sensor means for determining the air flow Φtot of the air which, in use, is supplied to the incinerator, the computer being arranged to determine on the basis of the measured fractions Xco2, X02 and XH20, the ash-free heating value (H W aste,a 8 h--τee,[J/kg ash-free]) and/or, further on the basis of the measured air flow Φtot, the amount of heat (Qheat,[W]) which is released upon the combustion. More particularly, it holds further that the computer is further arranged for further determining, on the basis of the predetermined value of the inert fraction of the waste (Xιnert,[kg inert/kg waste]), the following four parameters: the waste flow (Φwaste,[kg/s]), the moisture fraction of the waste (XH20, w ste, [kg water/kg waste]), the heating value of the total waste (H W aste, [J kg waste]) and/or the fraction of uncombusted (Xuncomt>usted,[kg uncombusted/kg ash]). On the basis of one or more of the above-mentioned parameters as determined by the computer, the waste incineration plant can be controlled in a manner known per se, such that combustion is optimal. The invention will presently be further elucidated with reference to the drawings. In the drawings: Fig. 1 shows a possible embodiment of a plant for waste incineration comprising a system according to the invention; and Fig. 2 shows a simplified representation of the waste incineration process of the system according to Fig. 1. In Fig. 1, a plant for waste incineration is designated by reference numeral 1. The plant comprises an incinerator 2, known per se, comprising an entrance 4 to which the waste is supplied. The incinerator 2 further comprises an exit 6 for discharge of the combustion products formed upon combustion. The plant further comprises a conveying device 8 which conveys the waste for combustion from the entrance 4 to the exit 6. The plant in this example further comprises means 10, known per se, for controlling the amount of air and/or optionally the temperature of the air which is supplied to the incinerator. The plant further comprises a control unit 12, which in this example comprises a computer for controlling various settings of the incinerator. Thus the computer 12 can, for instance, control the air supply means 10 and/or the speed of the conveying device 8. These controls can, in this example, be carried out via line 14. The incinerator may further comprise a chimney 16 with a controllable outlet 18. The outlet 18 in this example is likewise controlled by the computer 12, via a line 20. In the chimney, further, a dust catcher 22 known per se is included. Via a conduit 24 at least a portion of the flue gases which leave the incinerator via the chimney 16 and which have been stripped of dust by means of the device 22 can be fed back to the incinerator. This involves so-called flue gas recirculation. Further, adjacent the chimney 16 an inlet 25 may be arranged via which inlet secondary air can be supplied to the incinerator. The computer 12 may further be arranged to control a control valve 28, arranged in the return conduit 24, via a line 26. In Fig. 2 the combustion process of the plant according to Fig. 1 is schematically indicated. The incinerator proper is represented here by a square. The waste that is supplied to the incinerator via the entrance is designated by reference numeral 30. The primary air that is supplied to the incinerator via the air supply means 10 is designated by reference numeral 32. The secondary air that is supplied via inlet 25 to the incinerator is designated by reference numeral 34. The flue gas that leaves the incinerator via the chimney 16 is designated by reference numeral 36, whilst the portion of the flue gas that is recirculated to the incinerator via the conduit 24 is designated by reference numeral 38. The portion of the waste that is not burnt in the incinerator is designated by reference numeral 40. Output streams therefore consist of the flue gas and the uncombusted waste. The waste consists of a fraction of combustible (CH y O z ), moisture and inert. The values of y and z are to be further determined. In the primary and secondary air, also the water present in the air is included. The composition of the flue gas recirculation is equal to the composition of the flue gas. It has been assumed that the uncombusted waste consists solely of carbon. The combustible part of the waste reacts with oxygen to form carbon dioxide, water and carbon. Here, a carbon conversion (Xc, [mol/mol]) is assumed. The fraction of moisture in the primary and secondary air can be calculated if the temperature and the relative humidity of the air are known. The saturated vapor pressure of water (P°H20,[Pa]) can be calculated using the temperature of the air (Ta , [K]). The fraction of moisture in the air (XH2o,air, [mol/mol]) can now be calculated using the relative humidity (RHair,[%]) and the total pressure (P, [Pa]). The fraction of oxygen and nitrogen in the air can now be calculated as follows. Xθ2,aιr = 0.2095 (1 - X H 20,a-r) (3) X Ν 2,air = 0.7905 (1 - X H 20,a-r) (4) If the other gases present in the flue gas are disregarded, the fraction of nitrogen in the flue gas (Km, [mol/mol]) can be calculated from the fraction of oxygen, water and carbon dioxide (X02, XH2O, XCO2, [mol/mol]): XN2 = 1 — X02 — XH20 — Xco2 (5) For calculating the waste composition using the mass balances, presently the following data are needed. First, the molar flow rates of the primary and secondary air and of the flue gas recirculation (Φ pπ maιy, Φ seco n d ary, Φrec-rcuiation, [mol s]). Next, it was chosen to fix the carbon conversion and a value for y. Realistic values for these constants will be discussed later on. The flue gas flow (Φ-iue as, [mol/s]) can be calculated using a mole balance over the nitrogen. XN2,-ur( Φpπmary"* " Φaecondary) "r "XN2 Φ recirculation— XN2 Φ flue gas (6) Describing this equation gives: Φfhegas — The molar flow of combustible (ΦcHyOz, [mol/s]) can be calculated using a mole balance over carbon: Φ cHyθz + X c02 Φ recirculation = X c02 Φ flue gas +(l ~ Xc . Φ cHyOz (8) Combination of the carbon balance and nitrogen balance yields Φ cHyOz ( Φ primary + Φ secondary) (9) XC. ΛM z can be calculated using the mole balance over oxygen. Xθ2.Φ aegαs + ~ .( 2.Xc + ~ y~ Z l.ΦcHyOz (10) Combination of the carbon balance, nitrogen balance and oxygen balance yields From this equation it follows that z is not dependent on the primary and secondary air flow rates (Φprimary, Φsecondary, and Φ-ot) and the flue gas circulation flow rates. For the calculation of z, only the flue gas composition needs to be measured. A logical consequence of this is that for instance leakage airs do not have any influence on the calculation of z either. In fact, additional air translates into a change of the flue gas composition, such that z remains equal. The molar flow of water in the waste (ΦH20, [mol/s] can be calculated using the mole balance over water: ΦH20 + X720, air.yΦpn aiy + Φ sec ondary) + X /20. Φre rculation + — .y. ΦcHyOz = X//20. Φfl egas 2 (12) Description of this equation gives: I Xtf20. -5-jv 2 , aiΛ 1 Xrø2. Xv2, _w ■ , . ΦH20 — \ — XH20, aιr — - . y. — — . ( Φprimary + Φ sec ondarv) (13) * ΛW2 2 Xc. ΛΛ'2 ' The mole mass of the combustible part of the waste (McΗ y θz,[kg/mol]) is equal to McHyθz=0.012+0.001 y+0.016 z (14) The heat of combustion of the combustible part of the waste (Hc H yθ z ,[J/kg]) can be calculated using Michel's equation: 408.4 + \02A.y- \ 56.8. z . ._. HcH = -— .10 3 (15) McH Oz Formula 15 too is independent of the flow rates mentioned. Next, it is chosen to characterize the combustion process on the basis of the ash-free waste composition. The inert part of the waste will therefore initially not be included in the calculations. There are two reasons for this. First, inclusion of the inert part introduces an additional uncertainty into the calculation because the exact value of the inert fraction is not known. Second, only the heat capacity of the inert part has any influence on the energy balance of the incinerator. This heat capacity, however, is small with respect to the total energy content of the incinerator. The moisture fraction based on the ash-free waste (XH2θ,ash-free, [kg water/kg ash-free] can now be calculated as follows: X 20, ashfree = — — (16) Φ/Y20. MH20 + ΦcHyO∑. MCHyOz Elaboration of this equation yields: H20 ', ashfree — 1 TVTTTTI-Γ- f X /20. Xc Xw20, αιr. Xc. -J- Ϋ2 I — ' — .y) (17) V V X Λ.CCΎ0; 2 2 X X.rCθ022.. XXNjV22,, aaiιrr -x 2 ) / From this equation, it follows that the moisture fraction is also independent of the flow rates. The ash-free heating value (Hwaste.ash-free,[J kg ash-free]) is now equal to: H eva p is the evaporative value of water and is equal to 2,444, 10 6 J kg. The ash- free heating value can therefore be calculated if the flue gas composition is measured and if a particular value is chosen for y and Xc. Also needed are the constant values determined on the basis of the formulae 1 to 4. The amount of heat (Qheat,[W]) which is released upon the combustion is equal to: ΦcHvOz. McHyOz (Xheal == lwasle , ashfree (19) 1 — XH20, ashfree If the inert fraction of the waste (Xmert, [kg inert kg waste]) is known, the following four calculations can be carried out. First, the waste flow (Φ W aste,[kg/s]) can be calculated using the following formula: ΦcHyOz. McHyOz + ΦH20. MH20 Φwaste = " (20) 1 — Xmert The moisture fraction of the waste (Xri2θ,[kg water/kg waste]) can now be calculated as follows: The heating value of the total waste (H wa st e , [J/kg waste]) is now equal to: For this heating value, in principle the same holds true as for the ash-free heating value. The heating value of the total waste is independent of the value of the flow rates. The fraction of uncombusted (Xuncombusted, [kg C kg ash]) can be calculated using the following relation: (l - Nc).0.012 Xuncombusted * (23) McHyOz. Xmert + (l - Nc).0.012 1 — Λ. inert — Λji20, waste Since it has been chosen to fix the y value, an analysis of the waste composition was carried out. On the basis of the standard composition of waste as used in the FACE model, an estimate of the variation in y and z was made. In Table 1 the composition of different components of combustible is represented. Table 1: Standard composition of the FACE model On the basis of the data from Table 1, the values of y and z for the different components can be calculated. These values are represented in Table 2. Table 2: y and z values of CHyOz for combustible components The value of y therefore varies at a maximum between 1.6 and 1.8 and the value of z between 0.0 and 0.7. On the basis of the waste composition of the waste in random waste incineration plants, an estimate was made of the average waste composition. In Table 3, three different waste compositions are represented in which the plastic and GFT (Negetables/Fruit/Garden Refuse) fraction are strongly varied. Table 3: Waste composition Accordingly, the value of y is fairly constant for different waste compositions. A good estimate of y is 1.72. Another fixed variable is the carbon conversion. The value of X « is directly coupled to the percentage of uncombusted. In practice, this value varies between 0 and 5%, which corresponds to a value of 1 to 0.95 for X c . A good estimate of X« is 0.98. The plant according to Fig. 1 further comprises sensor means for measuring the concentrations of CO2, O 2 , and H 2 O in the flue gas. Further, the sensor means 42 are suitable for measuring the concentration of the flue gas. Thus, on the basis of the concentration of CO 2 and the concentration of the flue gas, the fraction Xco2 is known. The fraction X C0 2 indicates the number of moles of CO2 per mol of flue gas. Entirely by analogy, therefore, the fractions X02 and XH 2 O in the flue gas are known. The information obtained by means of the sensor means is supplied via line 44 to the computer 12. The computer 12 is arranged for determining, on the basis of the fractions Xco2, X02 and XH20 in the flue gas, the composition (y/z) and/or the heating value (HcH y oz,[J kg]) of the combustible part CH y O z of the matter supplied to the system. In use, the computer calculates the value of z on the basis of the formulae: 1 2. Xc.XN2. Xθ2,aιr 2. Xc. Xθ2 z = 2.Xc + -.y —— + ——- — (11) 2 Xcθl. XN .aιr XcOl and XΝ2 ■ = 1 — X02 — XH20 — Xcθ2 (5) The predetermined constant values Xo2,air and XN2,air can be determined beforehand on the basis of the formulae 1 to 4 and be inputted into the computer. Also, an estimate of the value of y can be inputted into the computer beforehand. As noted, a good estimate is y = 1.72. An estimate of the carbon conversion Xc can also have been inputted into the computer beforehand. As noted, a good estimate is Xc = 0.98. In use, the computer calculates the value of HcHyOz. 408.4 + 102.4. v - 156.8.z , YiCHyOz = — ~ .10 3 (15) CHyOz and McHyθz=0.012+0.001 y+0.016 z (14) The system further comprises sensor means 46 and 48, schematically indicated in Fig. 1, for respectively determining the flow rate Φpr m ry of the primary amount of air which is supplied to the incinerator by means of the air supply means 10, as well as the flow rate Φsecon ary of the secondary amount of air which is supplied to the incinerator via the inlet 25. The sensor means 46 and 48 are likewise connected to the computer 12 for transmitting the flow rates to the computer. The computer 12 is arranged for determining the total flow rate of the air supplied to the incinerator, with Φ to t = Φprimary + Φsecondary. The computer is further arranged for determining on the basis of the measured fractions Xco2, X02 and XH20 as well as the measured air flow Φtot, the ash-free heating value H waste , ash -fr ee ,[J/kg ash-free]) and/or the amount of heat (Qheat, [W]) which is released upon the combustion. More particularly, in use, the computer determines the ash-free heating value Hwaste.ash -ree on the basis of the formula: * ™ //20 ΛM2U, ashfree — 1 Mττιn+ [ Xn20.Xc X /20, air. Xc. XiV2 . V Xco 2 XCO2. XΛ'2, air XX (17) wherein MH2 0 represents the molar mass of water and H e a P the evaporative heat of water. It is noted that for calculating the other heating values the value of Φ to t is not relevant. The constant values for MH20 and H ev a P have been priorly inputted into the computer. Further, the computer determines, in use, the amount Qheat which is released upon the combustion, on the basis of the formulae: ΦcHyOz. McHyOz Qheat = Hwasie, ashfree ~ — J and (19) 1 — XH20, ashfree Φ cHyOz ( Φprimary + Φ secondary) (9) For carrying out this calculation, the measured value of Φ to t therefore is relevant. The computer is further arranged to determine, on the basis of the predetermined value of the inert fraction of the waste (X-ne-t, [kg inert/ kg waste]), the following four parameters on the basis of the formulae 20 to 23, respectively: the waste flow (Φ W aste,[kg/s]), the moisture fraction of the waste (XH20,waste,[k water/kg waste]), the heating value of the total waste (Hwaste, [J kg waste]) and/or the fraction of uncombusted (Xuncombusted, [kg C/ kg ash]). The computer therefore determines, in use, Φ aste on the basis of the following formula: ΦcHyOz. McHyOz + ΦH20. MH20 Φwaste ~ 1 — Xmerl In use, the computer calculates the value of Xmo on the basis of the following formula: Further, it holds that, in use, the computer calculates Hwaste on the basis of the following formula: Hwaste = (l — Xmert — XHX). HcHyOi — XH20. H evap , Also, it holds that, in use, the computer determines Xuncombusted on the basis of the following formula: (1 - Xc).0.012 Xuncombusted — ~ ~ 7 ~ (2θ) McHyUZ. Xmert , . — + (1 - Nc).0.012 1 — Λinerl — ΛH20, waste In the system, the computer can control the waste incineration process on the basis of one or more of the parameters calculated. Thus, for instance, on the basis of the determined amount of heat released upon the combustion (Qheat), the ash-free heating value (Hwaste, ash-free) and/or the heating value of the total waste (H wβ ste), it is possible to control the amount of air and/or the temperature of the air which is supplied to the incinerator 2 by means of the air supply means 10, 25. Also, on the basis of other parameters which have been calculated using the computer 2, these and/or other settings of the incinerator can be controlled, such as the speed of the conveying means 8, a metering slide of the entrance 4, the setting of the valves 18, 28, and so forth. Such variants are each understood to fall within the scope of the invention.

Claims: CLAIMS 1. A system for determining process parameters relating to thermal combustion processes of matter such as, for instance, waste in an incinerator, comprising sensor means and a computer coupled thereto for determining the parameters, wherein, in use, matter having a combustible part CHyOz is supplied to the incinerator and combusted, thereby forming a flue gas, characterized in that the sensor means are arranged for measuring the fractions Xco2, X02 and XH20 in the flue gas and that the computer is arranged for determining, on the basis of the measured fractions, the composition (y/z) and/or the heat of combustion (HcHyOz, [J kg]) of the combustible part CH y O z , with X02, XH20, Xco2 respectively representing the fractions of O2, H2O and CO2 in the flue gas. 2. A system according to claim 1, characterized in that, in use, the computer calculates the value of Z on the basis of the formulae: and XΝ2 = 1 — X02 — XH20 — XC02 (5) wherein Xo2,arr (the oxygen fraction in air supphed to the incinerator), XN 2 ,a-r (the nitrogen fraction in air supphed to the incinerator), Xc (the uncombusted fraction of carbon) and y are predetermined constant values. 3. A system according to claim 2, characterized in that the predetermined value Xc is between 0.90 and 1. 4. A system according to claim 2 or 3, characterized in that, in use, the computer calculates the value of HcH Oz on the basis of the formulae: , cHyo. .10 3 (15) and 5. A system according to any one of the preceding claims, characterized in that the system further comprises sensor means for determining the air flow Φ to t of the air which, in use, is supplied to the incinerator, the computer being arranged to determine on the basis of the measured fractions Xco2, X02 and Xκ-20, the ash-free heating value (H wa βte,as h f ree, [J/kg ash-free]) and/or, further on the basis of the measured air flow Φtot, the amount of heat (Qheat, [W]) which is released upon the combustion. 6. A system according to claim 4 or 5, characterized in that, in use, the computer determines the ash-free heating value H w --βte,a-.h-free on the basis of the formulae: and M -720 X/720, ashfree = * M H 20+ McHyOz XH20. Xr X/-T20, air. Xc. XN2 1 " \ X.C ~ 02 - vC02. vXN —2, aιr - ~ 2 - y J) (17) wherein MH20 represents the known molar mass of water and H eV ap represents the known evaporative heat of water. 7. A system according to claims 5 and 6, characterized in that, in use, the computer determines the amount of heat Qheat which is released upon the combustion, on the basis of the formulae: ΦcHvOz. McHyOz heat = Hwaste, ashfree (19) 1 — XH20, ashfree and ( Φ primary + Φ secondary) (9) 8. A system according to any one of claims 5-7, characterized in that the computer is further arranged for determining, on the basis of the predetermined value of the inert fraction of the waste (Xinert,[kg inert/ kg waste]), the following parameters: the waste flow (Φwaste, [kg/s]), the moisture fraction of the waste (XH20, w a ste, [kg water/kg waste]), the heating value of the total waste (Hwaste, [J/kg waste]) and/or the fraction of uncombusted (Xuncombusted, [kg C/kg ash]). 9. A system according to claim 8, characterized in that, in use, the computer determines Φwaste on the basis of the following formula: ΦctfyOz. McHyOz + ΦH20. M 20 Φwaste = " (20) 1 — Xmert 10. A system according to claim 9, characterized in that, in use, the computer calculates XH20, waste on the basis of the following formula: Φtøo. Miio mo = ^ ^ 1 ( 2D 11. A system according to claim 10, characterized in that, in use, the computer calculates Hwaste on the basis of the following formula: 12. A system according to claim 10 or 11, characterized in that, in use, the computer determines Xuncombusted on the basis of the following formula: (1 - Nr).0.012 Xuncombusted — (2ι ) McHyUZ. Xmert , - -— - + (1 - N )-0.012 i — Λinerl — ΛH2(), waste

Inventors: BREM GERRIT, VAN KESSEL LAMBERTUS BERNARDUS, BREM, GERRIT, VAN KESSEL, LAMBERTUS, BERNARDUS, MARIA
Applicants: BREM GERRIT, KESSEL LAMBERTUS BERNARDUS MAR, TNO, BREM, GERRIT, NEDERLANDSE ORGANISATIE VOOR TOEGEPAST-NATUURWETENSCHAPPELIJK ONDERZOEK TNO, VAN KESSEL, LAMBERTUS, BERNARDUS, MARIA
Application year: 2000
Main classification: F23G5
IPC codes: F23G5, F23N1, F23N5, G06F17