ARRANGEMENT AND PROCESS FOR CARRYING OUT AN INTENSIFIED COMBUSTION

Abstract

The invention relates to a combustion engine and to a process for producing energy by means of expansion work in combustion engines. The invention is based on the problem of providing a possibility for supplying oxygen to the combustion space of a self-compacting combustion engine in an energy-efficient manner. According to the invention, with an arrangement for carrying out an intensified combustion for automatically increasing pressure of the combustion gases and using them in a combustion engine for performing mechanical work, the above-stated problem is solved in that an oxygen storage material is present in the combustion space so that a self-compressing combustion process is made possible by storing the oxygen in the oxygen storage material in the combustion space.

Claims

1.-11. (canceled)

12. An arrangement for carrying out an intensified combustion for automatically increasing pressure of combustion gases and use thereof in a combustion engine for performing mechanical work, wherein the arrangement comprises an oxygen storage material which is provided in a combustion space.

13. The arrangement of claim 12, wherein the combustion space comprises at least two reaction chambers, each reaction chamber containing an oxygen storage material, comprising at least one input for a fuel and at least one input for fresh air, comprising a first output for giving off oxygen-depleted air, comprising a second output which is provided with a valve for giving off combustion gases, each second output communicating via an input with a downstream work chamber, wherein only one valve is opened in each instance for introducing the combustion gases into the downstream work chamber.

14. The arrangement of claim 12, wherein the oxygen storage material has a reduction enthalpy for oxygen removal of from 150 kJ/mol of O.sub.2 to 350 kJ/mol of O.sub.2.

15. The arrangement of claim 13, wherein the oxygen storage material has a reduction enthalpy for oxygen removal of from 150 kJ/mol of O.sub.2 to 350 kJ/mol of O.sub.2.

16. The arrangement of claim 12, wherein the oxygen storage material comprises a granulate of Ca.sub.0.5Sr.sub.0.5Mn.sub.0.5Fe.sub.0.5O.sub.3- with an open porosity of 30 percent by volume and a density of 3.67 g/cm.sup.3.

17. The arrangement of claim 13, wherein the oxygen storage material comprises a granulate of Ca.sub.0.5Sr.sub.0.5Mn.sub.0.5Fe.sub.0.5O.sub.3- with an open porosity of 30 percent by volume and a density of 3.67 g/cm.sup.3.

18. The arrangement of claim 12, wherein the combustion space comprises one or more reaction chambers and each reaction chamber comprises a further input for injecting liquid water or gaseous water for internal cooling of the oxygen storage material and of an interior of the reaction chamber and for increasing a pressure of the combustion gases.

19. The arrangement of claim 13, wherein each reaction chamber comprises a further input for injecting liquid water or gaseous water for internal cooling of the oxygen storage material and of an interior of the reaction chamber and for increasing a pressure of the combustion gases.

20. The arrangement of claim 12, wherein the oxygen storage material is combined with a catalyst in order to increase a reaction rate or reduce a concentration of harmful substances.

21. The arrangement of claim 13, wherein the oxygen storage material is combined with a catalyst in order to increase a reaction rate or reduce a concentration of harmful substances.

22. The arrangement of claim 14, wherein the oxygen storage material is combined with a catalyst in order to increase a reaction rate or reduce a concentration of harmful substances.

23. The arrangement of claim 15, wherein the oxygen storage material is combined with a catalyst in order to increase a reaction rate or reduce a concentration of harmful substances.

24. The arrangement of claim 16, wherein the oxygen storage material is combined with a catalyst in order to increase a reaction rate or reduce a concentration of harmful substances.

25. The arrangement of claim 17, wherein the oxygen storage material is combined with a catalyst in order to increase a reaction rate or reduce a concentration of harmful substances.

26. A process for carrying out an intensified combustion for automatically increasing pressure of the combustion gases and use thereof in a combustion engine for performing mechanical work, wherein the method comprises storing an oxygen storage material in a combustion space, supplying fresh air, with the oxygen storage material extracting oxygen from the fresh air, subsequently supplying fuel, completely combusting the fuel with oxygen released by oxygen storage material to form combustion gases which are under high pressure and at high temperature, and using the combustion gases for performing mechanical work.

27. The process of claim 26, wherein the process is carried out using at least two reaction chambers and wherein (a) a first reaction chamber is supplied with fresh air so that the oxygen storage material present in the first reaction chamber extracts the oxygen from the fresh air; (b) after saturation of the oxygen storage material with oxygen, supply of fresh air is interrupted and a fuel is metered into the first reaction chamber and is completely combusted by oxygen released by the oxygen storage material; (c) combustion gases which are under pressure are supplied to a work chamber; (d) (a) to (c) are carried out consecutively for one or more of the at least two reaction chambers, the number of further reaction chambers being determined at least in that the first reaction chamber has interrupted its fresh air supply through saturation with oxygen.

28. The process of claim 26, wherein a temperature of the oxygen storage material is monitored and controlled by metering in varying amounts of water.

29. The process of claim 27, wherein a temperature of the oxygen storage material is monitored and controlled by metering in varying amounts of water.

30. The process of claim 26, wherein the process is carried out using at least two reaction chambers and wherein an air throughput in each reaction chamber is two to four times the amount that would be required in theory for reoxidizing the oxygen storage material in its entirety.

31. The process of claim 27, wherein an air throughput in each reaction chamber is two to four times the amount that would be required in theory for reoxidizing the oxygen storage material in its entirety.

Description

[0027] The invention will be described more fully in the following with reference to embodiment examples. The drawing shows:

[0028] FIG. 1 a schematic view of an SCC process.

[0029] According to FIG. 1, the substantial component parts of a combustion engine are three reaction chambers 1.1, 1.2 and 1.3 comprising in each instance stored oxygen storage material 2 and a work chamber 4 for performing the mechanical work. The work chamber 4 can be associated with a gas turbine which in turn drives a generator (not shown in FIG. 1) for generating electrical energy. A fan 5 is connected via pipes to each individual reaction chamber 1.1, 1.2 and 1.3 for supplying fresh air. Every reaction chamber 1.1, 1.2 and 1.3 has a first output 12.1, 12.2, 12.3 for discharging the oxygen-depleted air, a second output 3.1, 3.2, 3.3 for discharging the combustion gases and two further inputs. The one input 11.1, 11.2, 11.3 lets in the fuel and the other input 13.1, 13.2, 13.3 lets in water or water vapor.

EMBODIMENT EXAMPLE 1

[0030] Referring to FIG. 1, three reaction chambers 1.1, 1.2 and 1.3 are used for the self-compacting combustion of natural gas. Each reaction chamber 1.1, 1.2 and 1.3 has an inner volume of 1.8 liters which has been filled with 1 kg of oxygen storage material 2. A granulate of CSFMM5555 (Ca.sub.0.5Sr.sub.0.5Mn.sub.0.5Fe.sub.0.5O.sub.3-) with an open porosity of 30 percent by volume and a density of 3.67 g/cm.sup.3 is used for the oxygen storage material packed bed. The feedstock is produced via conventional ceramic mixed oxidetechnology and is subsequently mixed with potato starch as pore-former. The mass is molded through extrusion or continuous casting to strands with a diameter of about 4 mm and lengths of 10 to 15 mm. The sintering is carried out for 3 hours at 1430 C. The oxidation enthalpy of the oxygen storage material fabricated in this way is about 280 kJ/moles O.sub.2.

[0031] The three reaction chambers 1.1, 1.2 and 1.3 are connected in each instance via their second outputs 3.1, 3.2 and 3.3 to a work chamber 4 through pipes which are as short as possible and which have a small inner diameter. The pipes between fan 5 and reaction chambers 1.1, 1.2 and 1.3 have appreciably larger diameters in order to minimize pressure losses and enable large air throughputs at ambient pressure. All of the connection points between the pipes are outfitted with valves 6.1, 6.2, 6.3, 7.1, 7.2, 7.3 which can be formed as electromagnetic valves or check valves. A pressure reducing valve 9 is arranged at one input 8 of the work chamber 4. The outer surfaces of the reaction chambers 1.1, 1.2 and 1.3 are water-cooled and are connected to a cooling circuit. Additionally, all of the reaction chambers 1.1, 1.2 and 1.3 are outfitted with atomizer nozzles 10.1, 10.2, 10.3 for injection of liquid water or vapor.

[0032] The SCC process is started by heating up the reaction chambers 1.1, 1.2 and 1.3 with a natural gas burner, not shown. During the heating, at least an oxygen content of 5 percent by volume is realized in the exhaust gas in order to prevent a discharging of the oxygen storage material packing during heating. After a temperature of 650 C. is reached in the first reaction chamber 1.1, 4.8 standard liters of natural gas are injected into the latter via its input 11.1 at a pre-pressure of 15 bar. The combustion of the fuel consumes oxygen that is supplied by the oxygen storage material 2. In this way, the oxygen content z in the oxygen storage material packing is lowered from 2.84 to 2.70 (z in ABO.sub.z). The very rapidly progressing combustion generates a gas temperature of more than 3500 C. and a pressure of more than 110 bar. About 15 g of water are sprayed into the combustion zone in addition via another input 13.1 so that the combustion temperature decreases by about 800 K and the pressure increases to 210 bar. The combustion gases under high pressure and the vapor are conducted into the work chamber 4 which is a component part of a flow machine, which flow machine in turn drives a generator for generating electric current. The flow machine is constructed without a compression part and without a feed of combustion air, or these components are not utilized. When the pressure falls below 15 bar, natural gas is metered into the second reaction chamber 1.2 via its input 11.2 and combusted in the manner described above. The temperature of the oxygen storage material packings is permanently monitored and controlled in that varying amounts of water are metered in via the inputs 10.1, 10.2, 10.3. A maximum temperature of the oxygen storage material packing of 1200 C. is aimed for.

[0033] After every combustion process, the discharged oxygen storage material packing is regenerated with fresh air. Typically, the air throughput is two to four times the amount that would be required in theory for reoxidizing the oxygen storage material in its entirety. The surplus of cold air is used to keep the packing temperature at a constant level.

EMBODIMENT EXAMPLE 2

[0034] For a self-compacting combustion of benzene, three reaction chambers 1.1, 1.2 and 1.3 are used which have an inner volume of 0.6 liters in each instance. The reaction chambers 1.1, 1.2 and 1.3 are filled in each instance with 1 kg CaMnO.sub.3 in the form of a packing of mini-honeycombs which have a free volume of 65 percent by volume and a bulk density of 2.5 g/cm.sup.3. The feedstock is produced through conventional ceramic mixed oxide technology and molded through rigid plastic extrusion of an aqueously plasticized mass to form mini-honeycombs with dimensions of 88 mm, the strands being cut automatically into short pieces approximately 8 mm in length. The sintering is carried out at 1450 C. for 3 hours. The oxygen storage material mini-honeycombs are then coated with a water-based suspension of 20 mol % Gd.sub.2O.sub.3 and 75 mol % NiO to minimize carbonization of the surface. The coating is baked in for 2 hours at 1000 C. The oxidation enthalpy of the material fabricated in this way is about 300 kJ/mol of O.sub.2.

[0035] The three reaction chambers 1.1, 1.2 and 1.3 are connected to one another and to a work chamber 4 through pipes which are as short as possible and which have small inner diameters. The pipes between fan 5 and reaction chambers 1.1, 1.2 and 1.3 have appreciably larger diameters in order to minimize pressure losses and enable large air throughputs. All of the connection points between the pipes are outfitted with valves 6.1, 6.2, 6.3, 7.1, 7.2, 7.3. A pressure reducing valve 9 is arranged upstream of the work chamber 4. The outer surfaces of the reaction chambers 1.1, 1.2 and 1.3 are water-cooled and are connected to a cooling circuit. Additionally, all of the reaction chambers 1.1, 1.2 and 1.3 are outfitted with atomizer nozzles at inputs 10.1, 10.2, 10.3 for injection of liquid water or vapor.

[0036] The reaction chambers 1.1, 1.2 and 1.3 are first preheated to 600 C. through combustion of benzene under surplus air. Subsequently, the air supply is closed and 9 g of benzene are sprayed into the first reaction chamber 1.1. The atomized fuel ignites and is completely oxidized through the oxygen exiting from the oxygen storage material packing. The oxygen content z of the oxygen storage material mini-honeycombs is accordingly lowered from 2.95 to 2.65 (z in ABO.sub.z). The combustion gases increase in temperature to more than 4,000 K, the pressure increases to more than 800 bar. The gas temperature can be lowered by approximately 900 K by spraying in approximately 30 g of liquid water, and the pressure increases to 1600 bar.

[0037] As was already described in Embodiment Example 1, the gas under high pressure is used for generating current in a flow machine.

[0038] After every combustion process, the discharged oxygen storage material mini-honeycombs are regenerated with fresh air. The air throughput is typically two to four times the throughput required for the complete reoxidation of the oxygen storage material packing in its entirety. The surplus of cold fresh air is used to cool the oxygen storage material packing and the reaction chambers and to keep the temperature at a constant level.

[0039] There is a quantity of three reaction chambers 1.1, 1.2, 1.3 in Embodiment Examples 1 and 2. In principle, the quantity is determined by the temporal ratio between combustion phase and reoxidation phase. Since the combustion phase is considerably shorter than the reoxidation phase, a corresponding quantity of reaction chambers is selected to realize a substantially continuous gas flow at input 8 of work chamber 4.

LIST OF REFERENCE NUMERALS

[0040] 1.1 reaction chamber [0041] 1.2 reaction chamber [0042] 1.3 reaction chamber [0043] 2 oxygen storage material [0044] 3.1 second output [0045] 3.2 second output [0046] 3.3 second output [0047] 4 work chamber [0048] 5 fan [0049] 6.1 valve [0050] 6.2 valve [0051] 6.3 valve [0052] 7.1 valve [0053] 7.2 valve [0054] 7.3 valve [0055] 8 input (of the work chamber 4) [0056] 9 pressure reducing valve [0057] 10.1 atomizer nozzles [0058] 10.2 atomizer nozzles [0059] 10.3 atomizer nozzles [0060] 11.1 input (for fuel) [0061] 11.2 input (for fuel) [0062] 11.3 input (for fuel) [0063] 12.1 first output [0064] 12.2 first output [0065] 12.3 first output [0066] 13.1 input (for water or water vapor) [0067] 13.2 input (for water or water vapor) [0068] 13.3 input (for water or water vapor)