CN209848678U - SCR denitration system suitable for cement manufacture line kiln tail flue gas - Google Patents
SCR denitration system suitable for cement manufacture line kiln tail flue gas Download PDFInfo
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- CN209848678U CN209848678U CN201920541030.1U CN201920541030U CN209848678U CN 209848678 U CN209848678 U CN 209848678U CN 201920541030 U CN201920541030 U CN 201920541030U CN 209848678 U CN209848678 U CN 209848678U
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Abstract
The utility model relates to a SCR deNOx systems suitable for cement manufacture line kiln tail flue gas adds the branch road flue on high temperature flue, and the flue gas temperature that makes to get into the SCR reactor through the mode of drawing the flue gas that adjusts the temperature suits with catalyst window temperature, and then with NO in SCR deNOx reactorsxEfficiently and economically. The utility model discloses arrange SCR denitration reactor simultaneously behind kiln tail sack cleaner to at branch road cigaretteThe high-temperature dust remover is arranged on the way, so that smoke dust entering the SCR reactor is greatly reduced, the problem of catalyst blockage poisoning is solved, and the service life of the catalyst is prolonged. The system and the method provided by the utility model improve feasibility and economic nature of being applied to cement manufacture trade with SCR denitration technique, for cement manufacture line NOxThe improvement of the emission standard provides technical guidance, and has good economic benefit and application prospect.
Description
Technical Field
The utility model relates to a flue gas purification technical field, concretely relates to SCR deNOx systems suitable for cement manufacture line kiln tail flue gas.
Background
At present, NO of cement industry in ChinaxThe emission of NO accounts for the whole countryxAbout 10% of the total emission amount is discharged in the third place after thermal power generation and automobile exhaust emission. The 'atmospheric pollution emission Standard for Cement industry' GB4915-2013 currently executed in China requires NO of the existing and newly-built cement enterprisesxDischarge is less than or equal to 400mg/Nm3The key area is adjusted to be less than or equal to 320mg/Nm3. In some areas, even stricter emission standards are proposed, for example, the proposal of ultralow emission standard (survey for comments) of atmospheric pollutants in cement industry issued in 2018, 4.4 by environmental protection agency in Hebei province, and from 2020, 1.1.1.1 days, NO of cement manufacturing enterprisesxEmission of not more than 150mg/Nm3(ii) a 2017, Jiangsu province environmental protection hall issued about the development of non-electric industry NO of whole provincexThe notification of deep emission reduction requires NO before 2019, 6 months and 1 day in the cement industryxEmission not higher than 100mg/Nm3. Therefore, new technology and new process are urgently needed to meet the increasingly strict emission standard in the cement industry.
The industrial flue gas denitration process mainly adopts a selective non-catalytic reduction (SNCR) denitration technology and a Selective Catalytic Reduction (SCR) denitration technology, the SNCR technology commonly adopted by the cement kiln at present and NOxThe removal efficiency is about 60 percent, and the increasingly strict discharge standard is difficult to meet. The SCR flue gas denitration technology has the characteristics of mild reaction conditions, high denitration efficiency (90%), and the like, and is a relatively feasible technology. SCR is mature in the thermal power industry, but the working condition of a cement production line limits the application of SCR in the cement industry. The ash content of the tail flue gas of the cement kiln is high, so that the catalyst is easily blocked; the content of CaO in the smoke is high, and the CaO and SO in the smoke gas are mixed3CaSO produced by the reaction4The catalyst is covered on the surface of the catalyst, and the SCR catalyst is easily poisoned and deactivated.
In order to solve the problems of high dust in flue gas and easy poisoning of a catalyst, CN204543995U discloses a cement kiln tail low-temperature flue gas SCR denitration device, wherein the denitration device is arranged behind a cement kiln tail dust collector, purified flue gas passing through the kiln tail dust collector and supplied by a reducing agent supply system are sprayed into a reducing agent in a flue together with a reducing agent injection device arranged on a front flue of the low-temperature denitration device, the purified flue gas enters a medium-temperature denitration device filled with the catalyst after being uniformly mixed, is subjected to denitration and is discharged onto the flue in front of an inlet of a cement kiln tail exhaust fan, and finally the purified flue gas enters a kiln tail chimney for discharge. According to the technology, the SCR denitration reactor is arranged behind the dust collector, so that the problems of catalyst blockage, poisoning and the like are solved. However, the temperature of the flue gas entering the SCR denitration reactor is low, and although a low-temperature catalyst with the use temperature ranging from 80 ℃ to 150 ℃ is adopted, the research and development of the low-temperature catalyst are not mature at present, so that the application of the technology is limited.
CN107596917A discloses an SNCR-SCR device and a process for kiln tail flue gas of a cement clinker production line, ammonia water evaporation of an SCR denitration section is realized by using medium temperature flue gas (340-360 ℃) at the downstream of a kiln tail preheater, the ammonia water is mixed with low temperature flue gas (90-110 ℃) introduced from a kiln tail chimney through a dilution fan and then is sent into an SCR reactor, the temperature of the flue gas entering the SCR reactor meets the requirement of a conventional SCR catalyst, and the denitration reaction can be carried out efficiently. However, in the process, the SCR reactor is directly arranged behind the kiln tail preheater, and flue gas entering the reactor carries a large amount of dust, so that the SCR catalyst is easily blocked and poisoned, and the service life of the catalyst is shortened.
SUMMERY OF THE UTILITY MODEL
In view of the problems existing in the prior art, the purpose of the utility model is to provide a SCR deNOx systems suitable for cement manufacture line kiln tail flue gas utilizes NO in desorption cement kiln tail flue gas that this system can be high-efficient economicalxMeanwhile, the problem that the catalyst is easy to block and poison when the SCR technology is applied to the tail flue gas of the cement kiln is solved, and the service life of the catalyst is prolonged.
To achieve the purpose, the utility model adopts the following technical proposal:
the utility model provides a SCR deNOx systems suitable for cement manufacture line kiln tail flue gas, the system includes: the system comprises a kiln tail high-temperature flue 1, a main path flue 3, a waste heat boiler 4, a raw material mill 5, a bag-type dust remover 6, a flue gas heat exchanger 7, a branch flue 9, a high-temperature dust remover 10, a high-temperature fan 11, a flue gas regulating valve 12, a reducing agent injection device 13, an SCR reactor 14, a main fan 15 and a chimney 16;
the kiln tail high-temperature flue 1 is respectively connected with a main flue 3 and a branch flue 9, and the main flue 3 is sequentially connected with a waste heat boiler 4, a raw meal mill 5, a bag-type dust collector 6, a flue gas heat exchanger 7 cold air path, a reducing agent injection device 13, an SCR reactor 14, a main fan 15, a flue gas heat exchanger 7 hot air path and a chimney 16; the branch flue 9 is sequentially connected with a high-temperature dust remover 10, a high-temperature fan 11 and a flue gas regulating valve 12, and then is converged with the main flue 3 between the cold air path of the flue gas heat exchanger 7 and the reducing agent injection device 13.
In order to promote the flue gas temperature who gets into the reactor to the window temperature that suits with the catalyst, the utility model discloses be equipped with the branch road flue on the kiln tail high temperature flue that kiln tail preheater is connected, draw out the flue gas all the way and be used for adjusting flue gas temperature, this way temperature adjusting flue gas finally inward-remits on the main road pipeline before the denitration reactor. And a flue gas regulating valve is arranged on the branch flue, and the temperature-regulating flue gas volume can be regulated according to the required temperature.
The utility model provides an in the system, SCR denitration reactor arranges after kiln tail sack cleaner, is equipped with the high temperature dust remover on the branch road flue simultaneously, can reduce the smoke and dust that gets into the SCR reactor by a wide margin, has solved the catalyst and has blockked up the poisoning problem, has prolonged the life of catalyst.
The utility model discloses set up flue gas heat exchanger behind the main road sack cleaner, before main road flue gas and branch road flue gas mix. The main path flue gas treated by the bag-type dust collector enters a cold air path of the flue gas heat exchanger, and is heated and then is merged with the branch path temperature-adjusting flue gas; and the purified high-temperature flue gas treated by the SCR denitration reactor enters a hot air path of the flue gas heat exchanger through the main fan, and is discharged to the atmosphere through a chimney after being cooled.
Preferably, the system further comprises a reducing agent evaporation device 17, the reducing agent evaporation device 17 being connected to the reducing agent injection device 13. The reducing agent evaporator 17 can be selected according to the type of the selected reducing agent, and the utility model is not limited in particular.
Preferably, the high temperature dust collector 10 is any one of an electric dust collector, a bag-type dust collector or a cyclone dust collector.
Preferably, the type of the reducing agent injection device 13 is any one of a grid type, a swirl type, or a mixing type.
Preferably, the SCR reactor 14 includes baffles, sootblowers and a catalyst bed. The guide plate can uniformly mix the main path flue gas, the branch path temperature-adjusting flue gas and the sprayed reducing agent; the soot blower can be a sound wave soot blower or a steam soot blower, and preferably a steam soot blower; the catalyst bed layer can be selected from two for one, three for one or five for one, and the like, and can be specifically adjusted according to actual requirements.
Preferably, the kiln tail high-temperature flue 1, the main path flue 3 and the branch flue 9 are connected through a kiln tail high-temperature flue tee 2 and a flue gas mixing tee 8.
As an optimized technical scheme, the utility model discloses the method of utilizing above-mentioned SCR deNOx systems to carry out the denitration to cement manufacture line kiln tail flue gas can be for: kiln tail flue gas enters a kiln tail high-temperature flue 1 and then is divided into two paths, one path enters a main path flue gas pipeline 3, sequentially passes through a waste heat boiler 4 and a raw material mill 5, is dedusted by a bag-type deduster 6, and enters a flue gas heat exchanger 7 to exchange heat and heat in a cold air path; the other path of the flue gas enters a branch flue 9, sequentially passes through a high-temperature dust remover 10, a high-temperature fan 11 and a flue gas regulating valve 12, and then is merged with the main path flue gas after being heated up, the merged flue gas enters an SCR reactor 14 for denitration after being sprayed with a reducing agent through a reducing agent spraying device 13, and the flue gas after denitration and purification enters a hot air path of a flue gas heat exchanger 7 through a main fan 15 for heat exchange and temperature reduction, and then is discharged to the atmosphere through a chimney 16; wherein, the flue gas flow of the branch is adjusted by the flue gas adjusting valve 12, and the temperature of the converged flue gas is controlled to be adapted to the reaction temperature window of the catalyst in the SCR reactor 14.
Preferably, the temperature of the merged flue gas may be 200-.
Preferably, the temperature of the main flue gas at the merging is 150-.
Preferably, the temperature of the branch flue gas at the time of merging is 300-.
Preferably, the temperature of the merged flue gas is 200-240 ℃. The flue gas regulating valve on the branch flue can be regulated according to the actual required temperature of the catalyst window, the temperature of the flue gas entering the SCR reactor is regulated by controlling the entering amount of the temperature-regulated flue gas, so that the temperature of the flue gas is matched with the temperature of the reaction temperature window of the catalyst, and the removal efficiency is improved.
Preferably, the utility model discloses can adopt at least one in aqueous ammonia, urea or the liquid ammonia to carry out the denitration as the reductant.
As preferred technical scheme, the utility model provides a SCR deNOx systems can ally oneself with SNCR system and use for the denitration of cement manufacture line kiln tail flue gas.
At present, install SNCR deNOx systems on most domestic cement production lines, the utility model provides a system can install alone, also can with the present SNCR system ally oneself with usefulness on the production line, sharing reductant preparation facilities. After SNCR denitration, the load of an SCR reactor can be reduced, the number of catalyst bed layers can be properly reduced, and NO is improvedxThe removal efficiency is improved, and the operation cost is reduced.
Compared with the prior art, the utility model discloses following beneficial effect has at least:
(1) the utility model discloses introduced the branch road flue in current deNOx systems, drawn forth the flue gas of the same kind all the way and be used for adjusting flue gas temperature to accessible control flue gas flow carries out real-time regulation to flue gas temperature, has guaranteed that the flue gas temperature that gets into the SCR reactor suits with catalyst window temperature, makes the denitration reaction high-efficient go on.
(2) The utility model discloses arrange SCR denitration reactor behind kiln tail sack cleaner to set up the high temperature dust remover on the branch road flue, reduce the smoke and dust that gets into the SCR reactor by a wide margin, solve the catalyst and block up the poisoning problem, prolonged the life of catalyst.
(3) The utility model provides the high feasibility and the economic nature of being applied to cement manufacture trade with SCR denitration technique, for cement manufacture line NOxThe improvement of the emission standard provides technical guidance, and has good economic benefit and application prospect.
Drawings
Fig. 1 is a schematic structural diagram of an SCR denitration system suitable for kiln tail flue gas of a cement production line provided in embodiment 1 of the present invention;
in the figure: 1-kiln tail high-temperature flue, 2-kiln tail high-temperature flue tee joint, 3-main flue, 4-waste heat boiler, 5-raw meal mill, 6-bag dust collector, 7-flue gas heat exchanger, 8-flue gas mixing tee joint, 9-branch flue, 10-high-temperature electric dust remover, 11-high-temperature fan, 12-branch flue gas regulating valve, 13-reducing agent injection device, 14-SCR reactor, 15-main fan, 16-chimney and 17-reducing agent evaporation device.
The present invention will be described in further detail below. However, the following embodiments are only simple examples of the present invention, and do not represent or limit the scope of the present invention, which is defined by the appended claims.
Detailed Description
The technical solution of the present invention is further explained by the following embodiments with reference to the accompanying drawings.
To better illustrate the present invention, facilitating the understanding of the technical solutions of the present invention, typical but not limiting embodiments of the present invention are as follows:
example 1
This embodiment provides an SCR deNOx systems suitable for cement manufacture line kiln tail flue gas, as shown in fig. 1, the system includes: the kiln tail high-temperature flue 1 behind the kiln tail preheater is connected with a kiln tail high-temperature flue tee 2, and the flue is divided into two paths after passing through the tee: a main flue 3 and a branch flue 9;
the main flue 3 is sequentially provided with a waste heat boiler 4, a raw meal mill 5, a bag-type dust collector 6 and a flue gas heat exchanger 7, the bag-type dust collector 6 is connected with a cold air path of the flue gas heat exchanger 7, a reducing agent injection device 13, an SCR (selective catalytic reduction) reactor 14 and a main fan 15 are arranged behind the flue gas heat exchanger 7, and the main fan 15 is connected with a hot air path of the flue gas heat exchanger 7 and then connected with a chimney 16;
the branch flue 9 is sequentially provided with a high-temperature dust remover 10, a high-temperature fan 11 and a flue gas regulating valve 12, and then is converged between the flue gas heat exchanger 7 and the reducing agent injection device 13 with the main flue 3 through a flue gas mixing tee joint 8.
The system further comprises a reducing agent vaporizing device 17 connected to the reducing agent injection device 13 for vaporizing the reducing agent into the injection device.
The flue gas heat exchanger 7 comprises a cold air path and a hot air path, heat exchange is performed between the cold air path and the hot air path, the cold air path is used for heating up flue gas in the main path, and the hot air path is used for cooling down purified flue gas.
The high temperature dust collector 10 may be any one of an electric dust collector, a bag-type dust collector or a cyclone dust collector.
The type of the reducing agent injection device 13 may be any one of a grid type, a swirl type, or a mixing type.
The internal structure of the SCR reactor 14 includes a guide plate, a soot blower and a catalyst bed layer, wherein the soot blower can be a sound wave soot blower or a steam soot blower, and the catalyst bed layer can be selected from one with two, one with three or one with five.
Example 2
By utilizing the device provided by the embodiment 1, the denitration experiment is carried out on a 4500t/d novel dry-process cement kiln production line, and the SNCR denitration device is installed on the cement production line. Dust of high-temperature flue gas at kiln tailThe concentration is 60g/Nm3At a temperature of 380 ℃ NOxThe concentration is 300mg/Nm3Flue gas flow rate of 450000Nm3/h。
The main flue gas enters a main flue, heat is recovered through a waste heat boiler in sequence, raw materials are dried through a raw material mill, the flue gas enters a cold air path of a flue gas mixer after being dedusted by a bag-type dust remover, the temperature of the flue gas is 120 ℃, and the temperature of the flue gas at the outlet of the cold air path is 180 ℃ after heat exchange. The temperature-adjusted flue gas enters a branch flue, and the temperature of the flue gas reaching the flue gas junction point is 360 ℃ after the flue gas is subjected to high-temperature electric precipitation and a high-temperature fan. The catalyst with the reaction temperature of 220 ℃ is selected, the flow of the temperature-adjusting flue gas is controlled by using the flue gas adjusting valve, and the ratio of the main flue gas volume to the temperature-adjusting flue gas volume is adjusted to 3.5:1, so that the temperature of the main flue gas volume and the temperature-adjusting flue gas volume can be matched with the temperature of a catalyst reaction window. And spraying the merged flue gas into a reducing agent by a reducing agent spraying device, and then, allowing the flue gas to enter an SCR reactor for denitration, wherein the temperature of the denitrated flue gas is not changed greatly, the denitrated flue gas enters a hot air path of a flue gas heat exchanger by a main fan, the temperature of the flue gas is 120 ℃ after heat exchange, and the flue gas is discharged to the atmosphere by a chimney.
In the embodiment, 20% ammonia water is used as a reducing agent, a grid type reducing agent injection device is adopted, a catalyst bed layer adopts an arrangement mode of using three to prepare one, the aperture of the section of the catalyst is 0.5cm, a rake type steam soot blower is adopted, the soot blowing frequency is once a week, and NO in the discharged flue gas is removed after denitrationxHas a concentration of 32.5mg/Nm3。
Example 3
By utilizing the device provided by the embodiment 1, a denitration experiment is carried out on a 3200t/d novel dry-process cement kiln production line. The dust concentration of the kiln tail high-temperature flue gas is 40g/Nm3At a temperature of 360 ℃ NOxThe concentration is 420mg/Nm3Flue gas flow rate of 420000Nm3/h。
The main flue gas enters a main flue, heat is recovered through a waste heat boiler in sequence, raw materials are dried through a raw material mill, the flue gas enters a cold air path of a flue gas mixer after being dedusted by a bag-type dust remover, the temperature of the flue gas is 110 ℃, and the temperature of the flue gas at the outlet of the cold air path is 160 ℃ after heat exchange. The temperature-adjusted flue gas enters a branch flue, and the temperature of the flue gas reaching the flue gas junction point is 340 ℃ after the flue gas is subjected to high-temperature electric precipitation and a high-temperature fan. The catalyst with the reaction temperature of 200 ℃ is selected, the flow of the temperature-adjusting flue gas is controlled by using the flue gas adjusting valve, and the ratio of the main flue gas volume to the temperature-adjusting flue gas volume is adjusted to 3.5:1, so that the temperature of the main flue gas volume and the temperature-adjusting flue gas volume can be matched with the temperature of a catalyst reaction window. And spraying a reducing agent into the merged flue gas by a reducing agent spraying device, and then, allowing the flue gas to enter an SCR reactor for denitration, wherein the temperature of the denitrated flue gas is not changed greatly, the denitrated flue gas enters a hot air path of a flue gas heat exchanger by a main fan, the temperature of the flue gas after heat exchange is 115 ℃, and the flue gas is discharged to the atmosphere through a chimney.
In the embodiment, the reducing agent is urea, the reducing agent injection device is of a grid type, the catalyst bed layer is arranged in a three-to-one mode, the aperture of the section of the catalyst is 1.0cm, a rake type steam soot blower is adopted, and the soot blowing frequency is twice a week. After denitration, NO in discharged flue gasxHas a concentration of 38.2mg/Nm3。
Example 4
By using the device provided in example 1, a denitration experiment is carried out on a 2000t/d novel dry-process cement kiln production line. The dust concentration of the kiln tail high-temperature flue gas is 18g/Nm3At a temperature of 340 ℃ NOxThe concentration is 190mg/Nm3Flue gas flow rate of 28000Nm3/h。
The main flue gas enters a main flue, heat is recovered through a waste heat boiler in sequence, raw materials are dried through a raw material mill, the flue gas enters a cold air path of a flue gas mixer after being dedusted by a bag-type dust remover, the temperature of the flue gas is 110 ℃, and the temperature of the flue gas at the outlet of the cold air path is 150 ℃ after heat exchange. The temperature-adjusted flue gas enters a branch flue, and the temperature of the flue gas reaching the flue gas junction point is 320 ℃ after the flue gas is subjected to high-temperature electric precipitation and a high-temperature fan. The catalyst with the reaction temperature of 200 ℃ is selected, the flow of the temperature-adjusting flue gas is controlled by using the flue gas adjusting valve, and the ratio of the main flue gas volume to the temperature-adjusting flue gas volume is adjusted to 2.4:1, so that the temperature of the main flue gas volume and the temperature-adjusting flue gas volume can be matched with the temperature of a catalyst reaction window. And spraying the merged flue gas into a reducing agent by a reducing agent spraying device, and then, allowing the flue gas to enter an SCR reactor for denitration, wherein the temperature of the denitrated flue gas is not changed greatly, the denitrated flue gas enters a hot air path of a flue gas heat exchanger by a main fan, the temperature of the flue gas after heat exchange is 110 ℃, and the flue gas is discharged to the atmosphere by a chimney.
In the embodiment, liquid ammonia is used as a reducing agent, a grid type reducing agent injection device is adopted, a catalyst bed layer is arranged in a two-to-one mode, the aperture of the section of the catalyst is 1.5cm, a rake type steam soot blower is adopted, and the soot blowing frequency is twice a week. After denitration, NO in discharged flue gasxAt a concentration of 22.6mg/Nm3。
The applicant states that the present invention is described by the above embodiments, but the present invention is not limited to the above detailed structural features, i.e. the present invention can be implemented only by relying on the above detailed structural features. It should be clear to those skilled in the art that any modifications to the present invention, to the equivalent replacement of selected parts and the addition of auxiliary parts, the selection of specific modes, etc., all fall within the scope of protection and disclosure of the present invention.
Claims (7)
1. The utility model provides a SCR deNOx systems suitable for cement manufacture line kiln tail flue gas which characterized in that, the system includes: the system comprises a kiln tail high-temperature flue (1), a main path flue (3), a waste heat boiler (4), a raw meal mill (5), a bag-type dust remover (6), a flue gas heat exchanger (7), a branch flue (9), a high-temperature dust remover (10), a high-temperature fan (11), a flue gas regulating valve (12), a reducing agent injection device (13), an SCR reactor (14), a main fan (15) and a chimney (16);
the kiln tail high-temperature flue (1) is respectively connected with a main path flue (3) and a branch path flue (9), and the main path flue (3) is sequentially connected with a waste heat boiler (4), a raw meal mill (5), a bag-type dust collector (6), a flue gas heat exchanger (7) cold air path, a reducing agent injection device (13), an SCR reactor (14), a main fan (15), a flue gas heat exchanger (7) hot air path and a chimney (16); and the branch flue (9) is sequentially connected with a high-temperature dust remover (10), a high-temperature fan (11) and a flue gas regulating valve (12), and then is converged with the main flue (3) between the cold air path of the flue gas heat exchanger (7) and the reducing agent injection device (13).
2. The system according to claim 1, characterized in that the system further comprises a reducing agent evaporation device (17), which reducing agent evaporation device (17) is connected to a reducing agent injection device (13).
3. The system of claim 1, wherein the high temperature dust collector (10) is any one of an electric dust collector, a bag dust collector or a cyclone dust collector.
4. A system according to claim 1, characterized in that the reductant injection device (13) is of the type of any one of a grid type, a swirl type or a hybrid type.
5. The system of claim 1, wherein the SCR reactor (14) comprises baffles, sootblowers and catalyst beds.
6. The system according to claim 1, characterized in that the kiln tail high temperature flue (1), the main path flue (3) and the branch flue (9) are connected by a kiln tail high temperature flue tee (2) and a flue gas mixing tee (8).
7. The system according to claim 1, characterized in that the reducing agent in the reducing agent injection device (13) is at least one of ammonia, urea or liquid ammonia.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109876662A (en) * | 2019-04-19 | 2019-06-14 | 中国科学院过程工程研究所 | SCR denitration system and method for denitration suitable for cement producing line kiln exit gas |
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| CN109876662A (en) * | 2019-04-19 | 2019-06-14 | 中国科学院过程工程研究所 | SCR denitration system and method for denitration suitable for cement producing line kiln exit gas |
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