Device and method for introducing oxygen into a pressurized fluidized-bed gasification process

Abstract

The invention relates to an oxygen lance that has at least three mutually coaxial pipes, each of which delimits at least one annular gap. The outermost pipe is designed to conduct superheated steam and has a steam supply point, the central pipe is designed as an annular gap, and the innermost pipe is designed to conduct oxygen at a temperature of no higher than 180 C. and has an oxygen supply point. A temperature sensor is arranged within the innermost pipe, said temperature sensor extending to just in front of the opening of the innermost pipe. The innermost pipe tapers in the form of a nozzle before opening; the innermost pipe opens into the central pipe; and the opening of the central pipe protrudes farther relative to the opening of the outermost pipe.

Claims

1. An oxygen lance comprising: an inner pipe including an inlet disposed at a proximal end thereof, a mouth disposed at a distal end thereof, and a tapered nozzle section disposed upstream of said mouth; a middle pipe coaxially disposed around an outer surface of at least said distal end of said inner pipe and defining a middle annular gap between the outer surface of said inner pipe and an inner surface of said middle pipe, said middle pipe having a mouth disposed at a distal end thereof; an outer pipe coaxially disposed around an outer surface of at least a portion of said middle pipe and defining an outer annular gap between the outer surface of said middle pipe and an inner surface of said outer pipe, said outer pipe having an inlet disposed at a proximal end thereof and a mouth disposed at a distal end of said outer pipe beyond which said mouth of said middle pipe extends, wherein the outer pipe extends distally beyond a location within the middle pipe where the mouth of the inner pipe terminates; and a temperature probe disposed inside said inner pipe and having a distal end disposed upstream of said mouth of said inner pipe at said distal end thereof, wherein the temperature probe extends along a longitudinal axis of the inner pipe.

2. The oxygen lance of claim 1, wherein said mouth of said middle pipe is open.

3. The oxygen lance of claim 1, wherein said middle pipe includes a feed inlet and is configured to permit dry gas to flow through said middle pipe.

4. The oxygen lance of claim 3, wherein said middle pipe has a tapered nozzle section disposed upstream of said mouth of said inner pipe.

5. The oxygen lance of claim 1 wherein the inlet of the inner pipe is an inlet, wherein the inner pipe is configured to permit oxygen having a maximum temperature of 180 C. to flow there through from the inlet to the mouth, wherein the middle pipe is configured to permit oxygen to flow out of the mouth of the inner pipe and into the middle pipe, wherein the inlet of the outer pipe is a steam feed inlet, wherein the outer pipe is configured to permit superheated steam to flow through the outer pipe.

6. The oxygen lance of claim 1 wherein the temperature probe measures a temperature of a substance flowing through the inner pipe.

7. The oxygen lance of claim 1 wherein the middle pipe has a constant diameter at the location where the mount of the inner pipe terminates.

8. The oxygen lance of claim 1 further comprising a regulating valve disposed upstream of the inlet of the inner pipe for regulating an amount of gas or stopping gas from being fed into the inner pipe based on measurements from the temperature probe.

9. The oxygen lance of claim 1 wherein the mouth of the middle pipe that extends beyond the mouth of the outer pipe has a constant diameter.

10. A method for introducing oxygen into a fluidized bed gasification reactor operated according to the HTW method, comprising: providing an oxygen lance according to claim 1; feeding moist gas into the outer pipe at a pressure above a pressure in the fluidized bed gasification reactor; feeding oxygen into the inner pipe at a temperature of up to 180 C. and a pressure above a pressure in the fluidized bed gasification reactor; expelling the oxygen from the mouth of the inner pipe into the middle pipe; expelling an emerging free jet of gas from the mouth of the middle pipe, the emerging free jet of gas including at least the oxygen expelled from the inner pipe into the middle pipe; expelling moist gas from the mouth of the outer pipe as a cladding flow surrounding the mouth of the middle pipe and the associated emerging free jet of gas expelled therefrom, wherein a flow velocity of the emerging moist gas is higher than a flow velocity of oxygen expelled from the inner pipe.

11. The method of claim 10, further comprising: feeding dry gas into the middle pipe; mixing, in the middle pipe, the oxygen expelled from the inner pipe with the dry gas in the middle pipe, upstream of the mouth of the middle pipe, wherein said expelled emerging free jet of gas from said middle pipe is the mixed oxygen and dry gas; and expelling moist gas from the mouth of the outer pipe as a cladding flow surrounding the mouth of the middle pipe and the associated emerging free jet of gas expelled therefrom, wherein a flow velocity of the emerging moist gas is higher than a flow velocity of the mixed oxygen and dry gas expelled from the middle pipe.

12. The method of claim 10, wherein the moist gas is superheated steam.

13. The method of claim 10, wherein the moist gas is a mixture of carbon dioxide and superheated steam.

14. The method of claim 10, wherein the dry gas is carbon dioxide.

15. The method of claim 10, wherein the dry gas is nitrogen.

16. The method of claim 10, wherein the dry gas is a mixture of carbon dioxide and of air.

17. The method of claim 10, wherein the dry gas is a mixture of carbon dioxide and of nitrogen.

18. The method of claim 10, wherein the dry gas is not moved during operation.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) The present disclosure is described in detail below with reference to the attached drawing figure, wherein:

(2) FIG. 1 is a side cross section view of an embodiment of an oxygen lance of the present disclosure, the mouth of which is configured to be directed into the fluidized bed of a HTW gasification reactor.

(3) FIG. 2 is a schematic diagram depicting an embodiment of a layout for the supply lines for each of oxygen, carbon dioxide, and steam to be fed into an oxygen lance of the present disclosure.

DETAILED DESCRIPTION

(4) Disclosed herein is an oxygen lance having at least three pipes arranged coaxially, one at least partially disposed within in the other, and at least in each case delimiting an annular gap, wherein: the outermost pipe being designed for the conduction of superheated steam and having a steam feed point, the middle pipe being designed as an annular gap, the innermost pipe being designed for the conduction of oxygen with a temperature of at most 180 C. and having an oxygen feed point, there being arranged inside the innermost pipe a temperature probe which reaches to just short of the mouth of the innermost pipe, the innermost pipe tapering in a nozzle-like manner upstream of its mouth, the innermost pipe issuing into the middle pipe, and the mouth of the middle pipe projecting further in relation to the mouth of the outermost pipe.

(5) In one refinement, the middle pipe may be designed as a blind pipe closed on both sides, and in this case the term mouth used in the preceding paragraph is intended in this limiting instance to refer merely to the pipe end in the vicinity of the mouth of the outermost pipe. In another refinement, the middle pipe is open on the mouth side of the oxygen lance. In a further refinement, the middle pipe is designed for the conduction of dry gas and has a gas introduction point. In this case, in a further refinement, there may be provision whereby the middle pipe tapers in a nozzle-like manner upstream of the mouth of the innermost pipe issuing into the middle pipe.

(6) Dry gas is understood here, as is customary in combustion technology in contrast to steam generation technology, to mean an industrial gas without steam fractions. By contrast, moist gas is understood below to mean an industrial gas which also contains steam fractions, although this is not intended to mean that a multiphase mixture has been formed. Superheated steam is therefore to be considered as moist gas, even though it is dry in the sense that wet steam has not occurred.

(7) The object is also achieved, as described above, by means of a method for introducing oxygen into a fluidized bed gasification reactor, operated according to the HTW method, by means of an oxygen lance, moist gas being fed into the outermost pipe at a pressure above the pressure in the fluidized bed gasification reactor, oxygen being conducted into the innermost pipe at a temperature of at most 180 C. and with a pressure above the pressure in the fluidized bed gasification reactor, moist gas emerging from the mouth of the outermost pipe as a cladding flow around the mouth of the middle pipe and the emerging free jet, the flow velocity of the emerging moist gas being set higher than that of the emerging gas from the innermost pipe.

(8) In refinements of the method, there may be provision whereby dry gas is introduced into the middle pipe at a pressure above the pressure in the fluidized bed gasification reactor, and thereby oxygen and dry gas are intermixed upstream of the mouth of the middle pipe.

(9) In further refinements of the method, there is provision whereby the moist gas is superheated steam or a mixture of carbon dioxide and of superheated steam.

(10) In further refinements of the method, there is provision whereby the dry gas is carbon dioxide, nitrogen or a mixture of carbon dioxide and of air or a mixture of carbon dioxide and of nitrogen. Moreover, insofar as is desirable in the gasification process, operation without dry gas is possible, the positive effects upon the temperature of the moist gas being maintained. The minimum feed temperature of the dry gas into the middle pipe arises from the dew point of the moist gas used in the outermost pipe, this corresponding in the case of pure steam to the saturated steam temperature.

(11) It became apparent that this technical solution is especially beneficial economically, since the supply lines for carbon dioxide can be used due to the need to ensure inertization of the oxygen lances during rapid shutdowns, and the insertion of a further pipe into the oxygen lances entails only little outlay. The choice of a dry gas with high specific heat capacity and the additional shielding of the hot moist gas against the cooler oxygen prevent an appreciable lowering of temperature in the steam-carrying outermost pipe and therefore the condensation of steam in the outermost pipe.

(12) The invention is explained in more detail below by means of 2 sketches.

(13) FIG. 1 in this case shows diagrammatically a section through an oxygen lance, the mouth of which issues into the fluidized bed of an HTW gasification reactor, not shown, and

(14) FIG. 2 shows the circuitry of the supply lines for oxygen, carbon dioxide and steam.

(15) Oxygen 1 is conducted into the innermost pipe 2 in which the temperature measuring device 3 is arranged. The temperature amounts to 180 degrees Celsius and the pressure at the inlet to approximately 28 bar. The exact pressure is determined by means of the quantity control which feeds the reactor with exactly the quantity of oxygen just required instantaneously for gasification. Carbon dioxide 5 at 230 degrees Celsius is added to the middle pipe 4. Superheated steam 7 with a pressure of approximately 29 bar and a temperature of 410 degrees Celsius is introduced into the outermost pipe 6. This steam heats the carbon dioxide to a temperature of approximately 270 degrees Celsius, the oxygen likewise being heated slightly. Since the dew point of the steam is not in this case undershot, steam is not condensed out and no droplets are formed at the mouth 8 of the outermost pipe, so that a homogenous steam film can be formed around the tip of the oxygen lance.

(16) The oxygen of the innermost pipe and the carbon dioxide of the middle pipe are brought together at the mixing point 9 into a common gas stream, the feed point already lying inside the fluidized bed in the HTW gasification reactor. The mixture is conducted as a free jet 10 into the fluidized bed, the steam film preventing the oxygen from forming vortices around the nozzle tip and thus preventing possible local overheating with the result of ash softening and caking at the nozzle tip. The fluidized bed reactor can thereby be operated at a pressure of 28 bar.

(17) FIG. 2 shows a circuit diagram with supply lines for oxygen 11, carbon dioxide 12 and superheated steam 13 and also with the most important shut-off and regulating valves. In an emergency, carbon dioxide can be introduced into the oxygen line via the scavenging valve 14 and into the steam line via the regulating valve 15. As a rule, the two valves are closed. As a function of the oxygen quantity required, the regulating valve 16 serves for the oxygen supply, regulating valve 17 serves for regulating the quantity of carbon dioxide and the regulating valve 18 serves for the introduction of steam. Oxygen 11 can also be distributed to other nozzle levels via the oxygen distributor 19.

(18) The following computing and design examples illustrate the invention: In example 1, the outermost pipe is subjected to steam and the middle pipe to nitrogen. In example 2, the outermost pipe is subjected to steam and the middle pipe to carbon dioxide. In example 3, the outermost pipe is subjected to a mixture which is composed in equal proportions by mass of carbon dioxide and of steam and the middle pipe is subjected to carbon dioxide. In example 4, the outermost pipe is subjected to steam and the middle pipe is left without any throughflow.

(19) In all the examples, the innermost pipe is subjected to oxygen, the inside diameter amounting to approximately 25 mm and a thermocouple with a thickness of 11 mm being arranged inside. All the indications of dimension are approximate indications obtained from design calculations.

(20) TABLE-US-00001 Example 1 Example 2 Example 3 Example 4 gap of the outermost pipe [mm] 9 15 15 15 gap of the middle pipe [mm] 10 4 4 4 mass throughflow through the outermost 0.039 0.039 0.039 0.039 pipe [kg/s] mass throughflow through the middle pipe 0.0039 0.0039 0.0039 [kg/s] mass throughflow through the innermost 0.225 0.225 0.225 0.225 pipe [kg/s] inlet temperature into the outermost pipe 410 410 410 410 [ C.] inlet temperature into the middle pipe [ C.] 230 230 230 inlet temperature into the innermost pipe 180 180 180 180 [ C.] outlet temperature from the outermost pipe 400 390 390 390 [ C.] outlet temperature from the middle pipe 270 270 270 [ C.] outlet temperature from the innermost pipe 182 182 182 182 [ C.]

(21) In all instances, the saturated steam temperature of the moist gas of the outermost pipe is at no point undershot in the middle pipe, and therefore condensation cannot occur.

(22) The invention is not restricted to the examples illustrated, and, furthermore, it is also possible, in the case of different load situations or operating situations, to adapt the respective throughflows to the requirements in a flexible way.

LIST OF REFERENCE SYMBOLS

(23) 1 oxygen 2 innermost pipe 3 temperature measuring device 4 middle pipe 5 carbon dioxide 6 outermost pipe 7 steam 8 mouth of the outermost pipe 9 mixing point 10 free jet 11 oxygen 12 carbon dioxide 13 steam 14 scavenging valve 15 regulating valve 16 regulating valve 17 regulating valve 18 regulating valve 19 oxygen distributor