PROCESS AND PLANT FOR MANUFACTURING CEMENT IN THE OXYFUEL MODE

Abstract

Process for operating a cement or lime plant comprising a cement or lime kiln and a calciner, wherein heat is generated by combustion of a fuel in the kiln and/or calciner, wherein a gas fed to the kiln and the calciner or to the calciner for combustion of the fuel contains an oxygen rich exhaust gas from a bioreactor containing photoautotrophic organisms and wherein the plant is preferably operated in the oxyfuel mode by using exhaust gas from the kiln and/or calciner together with the oxygen from the bioreactor as the gas fed to the kiln and/or calciner for combustion of the fuel.

Claims

1. A process for operating a cement or lime plant comprising a cement or lime kiln (1, 11, 21, 31) and a calciner (2, 12) in case of a cement plant, wherein heat is generated by combustion of a fuel in the kiln (1, 11, 21, 31) and/or in the calciner (2, 12), wherein a gas fed to the kiln (1, 11, 21, 31) and the calciner (2, 12) or to the calciner (2, 12) for combustion of the fuel contains an oxygen rich exhaust gas from a bioreactor (4, 14, 24, 34) containing photoautotrophic organisms.

2. The process according to claim 1, wherein an exhaust gas from the kiln (1, 21) and/or calciner (2) is partly recycled into the kiln (1, 21) and/or calciner (2), operating the kiln (1, 21) and/or calciner (2) in the oxyfuel mode.

3. The process according to claim 2, wherein the gas fed to the the kiln (1, 21) and the calciner (2, 12) or to the calciner (2, 12) consists of the recycled exhaust gas from the kiln (1, 21) and/or calciner (2, 12) and the oxygen rich exhaust gas from the bioreactor (4, 14, 24).

4. The process according to claim 2, wherein the exhaust gas from the kiln (1, 11, 21, 31) and/or calciner (2, 12) that is not recycled into the kiln (1, 11, 21, 31) and/or calciner (2, 12) is passed into the bioreactor (4, 14, 24, 34) as feed gas for the photoautotrophic organisms.

5. The process according to claim 1, wherein the generated oxygen is partly stored during a time when the bioreactor (4, 24) generates oxygen and stored oxygen is fed to the kiln (1, 21) and/or calciner (2) during a time when the bioreactor (4, 24) does not generate oxygen.

6. The process according to claim 2, wherein the gas from the kiln (1, 21) and/or calciner (2) that is not recycled into the kiln (1, 21) and/or calciner (2), the vented gas, is stored during a time when the bioreactor (4, 24) does not generate oxygen and stored gas is fed to the bioreactor (4, 24) during a time when the bioreactor (4, 24) generates oxygen.

7. The process according to claim 1, wherein the exhaust gas from the kiln (11, 31) and/or calciner (12) is not recycled into the kiln (11, 31) or the calciner (12) and is passed into the bioreactor (14, 34) as feed gas for the photoautotrophic organisms.

8. The process according to claim 7, comprising the further step of enriching the exhaust gas in CO.sub.2 prior to passing it into the bioreactor (14, 34).

9. A cement or lime plant comprising a cement or lime kiln (1, 11, 21, 31), in the case of a cement plant a calciner (2, 12), and at least one burner for generating heat by combustion of a fuel in the kiln (1, 11, 21, 31) and/or in the calciner (2, 12), wherein it further comprises a bioreactor (4, 14, 24, 34) containing photoautotrophic organisms and means for passing oxygen generated by the organisms into the kiln (1, 11, 21, 31) and/or calciner (2, 12).

10. The cement or lime plant according to claim 9, wherein the cement or lime kiln (1, 11, 21, 31) and/or calciner (2, 12) is an oxyfuel kiln (1, 21) and/or oxyfuel calciner (2) receiving exhaust gas from the kiln (11, 21) and/or calciner (2) and the oxygen generated by the organisms as gas for the combustion of the fuel.

11. The cement or lime plant according to claim 10, further comprising devices for liquefying (5, 7) oxygen and exhaust gas from the kiln (1, 21) and/or calciner (2) that is not recycled into the kiln (1, 21) and/or calciner (2), the vented gas, containers (6, 8) for storing the liquefied oxygen and the vented gas, and devices for evaporating the stored oxygen and vented gas and feeding the oxygen into the kiln (1, 21) and/or calciner (2) and the vented gas into the bioreactor (4, 24), respectively.

12. Use of oxygen enriched exhaust gas from a bioreactor (4, 14, 24, 34) containing photoautotrophic organisms as full or partial replacement of air for combustion of a fuel in a kiln (1, 11) and/or a calciner (2, 12) of a cement plant or in a kiln (21, 31) of a lime plant.

Description

[0015] In the figures:

[0016] FIG. 1 shows an oxyfuel cement kiln supplied with oxygen from a bioreactor,

[0017] FIGS. 2a and 2b show an oxyfuel kiln and bioreactor with storage of the gases,

[0018] FIG. 3 shows a normal cement kiln supplied with oxygen from a bioreactor,

[0019] FIGS. 4a and 4b show a cement kiln with oxyfuel calciner,

[0020] FIG. 5 shows a shaft lime kiln and

[0021] FIG. 6 shows a rotary lime kiln.

[0022] In all figures the gas streams are shown with simple arrows and streams of solid material with wider arrows having a frame. Sunlight is depicted as wave. Inactive parts are shown in dotted lines.

[0023] FIG. 1 shows a cement plant operated in the oxyfuel mode comprising a cement kiln 1, a preheater or calciner 2 and a clinker cooler 3. The rest of the cement plant, like raw material feed for the kiln, corresponds to the known plants and is not shown or described, therefore. The bioreactor is designated 4.

[0024] The kiln 1 is operated in the oxyfuel mode, that means the gas entering the clinker cooler 3 does not contain any substantial amount of nitrogen, preferably it consists of oxygen and the recirculated gas containing unburnt oxygen and CO.sub.2. It contains only traces of other gases like nitrogen, argon and other components of air, that would require an inadequate expenditure to be removed. The recirculated CO.sub.2 is preferably dried. The gas entering the cooler 3 is preheated while the clinker cools. The preheated gas enters the kiln 1 where fuel is burnt to sinter the preheated or calcined raw meal to form the cement clinker which moves into the cooler 3. The hot gas is passed into the preheater/calciner 2, where the raw meal is preheated and usually also at least partly calcined. Typically, full calcination requires an additional burner.

[0025] The exhaust gas from the preheater/calciner 2 is recirculated to the cooler 3 and partly vented. Generally the vented gas contains 70% or more CO.sub.2 whereas the exhaust from a normal cement plant contains 20% to 25%.

[0026] In the shown embodiment, the vented gas is fed to the bioreactor 4 to be converted into valuable products by the organisms. In the bioreactor 4 photoautotrophic organisms convert CO.sub.2 into valuable products using sunlight as energy source. Besides the valuable product the organisms generate oxygen, which is added to the gas entering the cooler 3 according to the invention. The oxygen could of course also be added to the kiln inlet.

[0027] FIGS. 2a and 2b show a preferred embodiment of the invention. The parts which are identical to FIG. 1 have the same reference numbers and are not explained again. In addition to them, the device and process illustrated in FIGS. 2a and 2b uses a storage of oxygen and gas vented from the cement plant, designated CO.sub.2 in the following, to allow a 24 hours operation under similar conditions despite the lack of activity of the organisms in the bioreactor 4 during the night.

[0028] The day time operation is shown in FIG. 2a. Here the CO.sub.2 vented from the cement plant is fed directly into the bioreactor 4. The bioreactor 4 provides oxygen. A part of the oxygen is liquefied in device 5 and stored in container 6, the remaining amount is fed into the cooler 3 (or kiln inlet). Vented gas liquefied in device 8 and stored in container 9 during the night is evaporated in evaporater 10.

[0029] FIG. 2b shows the night time operation, where the bioreactor 4 does neither consume CO.sub.2 nor generate oxygen. During the night the oxygen needed for the kiln 1 (and preheater/calciner 2) is obtained by evaporating oxygen stored in container 6 in the evaporater 7. The CO.sub.2 vented from the cement plant is liquefied in device 8 and stored in container 9.

[0030] In all embodiments the process and device according to the invention can also be used when only the calciner is operated in the oxyfuel mode instead of the kiln and calciner. The CO.sub.2 reduction achieved with only an oxyfuel calciner in comparison to a normal kiln will be less than for the oxyfuel kiln but still considerable. The advantage is that the necessary changes to the plant are less. Since oxyfuel operation requires to keep out air, the demands on the tightness of the cooler, kiln and preheater/calciner are high. Restricting these requirements to the preheater/calciner section will lower the demands noticeably.

[0031] FIG. 3 shows a normal cement plant, i.e. not operated in the oxyfuel mode. This cement plant comprises a kiln 11, a preheater/calciner 12 and a clinker cooler 13. The difference in view of the oxyfuel plant is that air and not oxygen is fed into the cooler 13 and that no gas is recycled to the cooler 13, all is vented. As shown by the dashed arrow, combustion in the kiln 1 can be improved by feeding oxygen from the bioreactor 14 to the clinker burner in addition to air. It is also advantageous here to feed the vented gas which is enriched in CO.sub.2 into the bioreactor 14. The bioreactor will operate efficiently with exhaust gas with a CO.sub.2-concentration as low as 10%. However the exhaust gas of a regular operated kiln cannot be liquefied, and storage of the exhaust gas over night when it is gaseous would require unaffordable large storage facilities. Therefore, if full utilisation of the CO.sub.2 is envisioned, it is required to reach >70% CO.sub.2, so that liquefying is possible and storage of the CO.sub.2 as a liquid requires roughly 1000 times smaller storage facilities.

[0032] As noted previously, the bioreactor (4, 14) is only operating during day time while the cement plant runs 24 hours a day. Therefore, unless it is acceptable to operate the oxyfuel cement plant with differing conditions during night and day, some sort of oxygen supply has to be provided during the night. When no scheme as above described, i.e. a storage of part of the oxygen generated during the day, is possible or desired, oxygen supply as known in the art will be used during the night. The most common supply is by isolating oxygen from the ambient air, e.g. with the Linde process or some improved method.

[0033] Another possible approach is generation of oxygen by electrolysis of water, wherein it is desirable to utilize the hydrogen generated concurrently for converting the CO.sub.2 to valuable products. Such a process is described e.g. in WO 2015/055349 A1.

[0034] With regard to the bioreactor (4, 14), the most preferred photoautotrophic organisms are ones of the type described in WO 2009/036095 A1 and WO 2010/044960 A1. These produce the valuable end product, for example ethanol, directly. However, is is also possible to rely on other known processes and organisms, like algea, that utilize light and CO.sub.2 to build up biomass that is subsequently converted into the desired valuable end products.

[0035] For an exemplary oxyfuel kiln the mass balance for oxygen and carbon dioxide has been calculated and is shown in the following table 1.

TABLE-US-00001 TABLE 1 clinker production 125 tons/hour oxygen needed (according to Technical 35 tons/hour Report TR ECRA 119/2012) CO.sub.2 generated (865 kg/ton clinker) 108 tons/hour CO.sub.2 uptake (assumed uptake efficiency of 92 tons/hour CO.sub.2 85%) ratio of produced O.sub.2 to CO.sub.2 for ethanol 1.09 producing cyano bacteria ratio of produced O.sub.2 to CO.sub.2 for micro-algae 1.7 lower limit oxygen production 100 tons/hour

[0036] It can be seen, that for a typical cement kiln and a bioreactor dimensioned to be fed all the CO.sub.2 evaporated from the kiln operated in the in oxyfuel mode at least 65 tons/hour oxygen are available for storage and/or other uses.

[0037] FIGS. 4a and 4b show a cement plant wherein only the calciner 2 is operated in the oxyfuel mode while the kiln 1 receives air for combustion, which is preheated in the cooler 3. The bioreactor 4 providing oxygen for the calciner 2 as well as the devices for oxygen and carbon dioxide liquefying, storage, and evaporation 5, 6, 7 and 8, 9, 10 are the same as in the embodiment shown in FIGS. 2a and 2b. Heated air from the cooler 3 and/or the kiln 1 can in the embodiment of FIGS. 4a and 4b advantageously be passed into the raw materials and/or fuel drying.

[0038] The process according to the invention for operating a cement plant comprising a cement kiln and a calciner, wherein heat is generated by combustion of a fuel in the kiln and/or calciner, uses as gas for combustion of the fuel an oxygen rich exhaust gas from a bioreactor containing photoautotrophic organisms. Thereby, a cost effective source of oxygen is provided for improving combustion in the cement plant and utilizing the oxygen rich exhaust gas from the bioreactor generates an additional economical benefit for the reactor-plant.

[0039] In the preferred embodiment the cement plant is operated in the oxyfuel mode by using exhaust gas from the kiln and/or calciner together with the oxygen from the bioreactor as the gas fed to the kiln and/or calciner for combustion of the fuel. Thereby, a cost effective source of oxygen is provided for the oxyfuel cement plant and the gas vented from the cement plant is converted into valuable products by the organisms in the bioreactor.

[0040] The illustrated devices and methods can be applied analogously to the manufacturing of lime as shown in FIGS. 5 and 6.

[0041] FIG. 5 shows a vertical shaft kiln 21 for lime production in the oxyfuel mode combined with a bioreactor 24. Calcium carbonate, e.g. limestone, is fed as raw material at the upper end into the kiln 21. The upper part of the kiln 21 forms a preheating zone 22 where the raw material is preheated by the hot gases flowing upwards, a typical temperature is about 1200 K. The exhaust gas, comprising carbon dioxide and remaining oxygen, is passed out of the kiln at the upper end and is partly recycled into the lowest part of the kiln 21, which forms the cooling zone 23. The carbon dioxide that has to be vented is fed to the bioreactor 24. The preheated raw material passes down the kiln 21 into the burning zone 25 which is located in the middle of the kiln 21 and has a typical temperature of about 1500 K. Typically fuel and oxygen are fed into the kiln 21 at the burning zone 25 via lances 26. The oxygen is provided by the bioreactor 24 and fed to the cooling zone 23 and/or the burning zone 25. The raw material is decomposed into lime and carbon dioxide in the burning zone 25 and the lime then passes downwards through the cooling zone 23 and is taken out at the product outlet 27. Recycled exhaust gas and/or added oxygen from the bioreactor are passed into the cooling zone 23 for cooling. The introduced gas is usually heated to a temperature of 600 to 750 K by the lime leaving the burning zone 25 at about 1200 K.

[0042] FIG. 6 illustrates the manufacturing of lime in a rotary kiln 31. In this embodiment the kiln 31 is not operated in the oxyfuel mode and the oxygen produced by the bioreactor 34 may be used to improve the burning conditions in the kiln 31. The lime rotary kiln 31 has no separate preheater/calciner, the raw materials are fed directly into the kiln 31, so that preheating and burning (decomposition) both take place inside the kiln 31. The lime is cooled in cooler 33 by air and/or the oxygen from the bioreactor 34 that is passed into the kiln 31 in counterflow to the raw material. Exhaust gas from the kiln 31 is fed to the bioreactor 34, optionally after concentrating it in CO.sub.2.

[0043] Of course, the lime plants may be equipped with the same oxygen and/or carbon dioxide storage devices as the cement plants described before. Also the same methods of providing oxygen and using carbon dioxide during the night can be applied.

REFERENCE NUMBERS

[0044] 1 cement kiln [0045] 2 preheater/calciner [0046] 3 clinker cooler [0047] 4 bioreactor [0048] 5 oxygen liquefier [0049] 6 oxygen storage container [0050] 7 oxygen evaporater [0051] 8 CO.sub.2 liquefier [0052] 9 CO.sub.2 storage container [0053] 10 CO.sub.2 evaporator [0054] 11 cement kiln [0055] 12 preheater/calciner [0056] 13 clinker cooler [0057] 14 bioreactor [0058] 21 lime shaft kiln [0059] 22 preheating zone [0060] 23 cooling zone [0061] 24 bioreactor [0062] 25 burning zone [0063] 26 lance for fuel and air/oxygen [0064] 27 product outlet [0065] 31 lime rotary kiln [0066] 33 cooler [0067] 34 bioreactor