CN214223046U - Nitric acid system capable of generating high-temperature and high-pressure steam - Google Patents
Nitric acid system capable of generating high-temperature and high-pressure steam Download PDFInfo
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- CN214223046U CN214223046U CN202022516146.5U CN202022516146U CN214223046U CN 214223046 U CN214223046 U CN 214223046U CN 202022516146 U CN202022516146 U CN 202022516146U CN 214223046 U CN214223046 U CN 214223046U
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Abstract
The utility model discloses a nitric acid system capable of generating high-temperature and high-pressure steam, which comprises a steam turbine, wherein the steam turbine is connected with a steam drum through a condenser and an economizer in sequence, and the steam drum is connected with an oxidation furnace; the economizer is used for heating the condensed water to become saturated water and sending the heated saturated water into the steam pocket; the steam drum conveys the heated saturated water to the oxidation furnace for heating through a boiler water circulating pump, the saturated water is changed into supersaturated water and is conveyed back to the steam drum, and the steam drum is used for vaporizing the supersaturated water into saturated water and saturated steam and conveying the saturated water to the oxidation furnace through a pipeline; the oxidation furnace is used for recovering heat released by the ammonia oxidation reaction of air and ammonia, heating saturated water from the steam drum to be supersaturated water, heating saturated steam from the steam drum to be superheated steam, and outputting the supersaturated water and the superheated steam to the steam drum. The utility model discloses an improve the steam quality of oxidation furnace product, reduce nitric acid manufacturing cost, increase the quality and the transport capacity of delivering steam outward simultaneously, improve the economic benefits of enterprise.
Description
Technical Field
The utility model belongs to the technical field of nitric acid production equipment, concretely relates to can produce nitric acid system of high temperature high pressure steam.
Background
At present, the technological process of producing nitric acid belongs to the ammonia oxidation absorption method for preparing nitric acid. Five steps of purification of raw gas, ammonia catalytic oxidation, oxidation and absorption of ammonia oxide into acid, bleaching and tail gas treatment, gas compression and energy recovery are followed. The current domestic methods for producing dilute nitric acid comprise: synthetic, low pressure, full medium pressure, full high pressure and dual pressure processes. Wherein, the synthesis method and the low-pressure method are forbidden to be newly built due to the problems of high production cost, environmental protection and the like, and the full medium-pressure method is caused by tail gas NOXIf the concentration is too high, the ammonia can be discharged after reduction treatment, and the investment and operation cost for treating tail gas are high, so that the product cost is high, and the tail gas is gradually eliminated. The double-pressurization method technology is a preferred technology for nitric acid devices in many enterprises due to the characteristics of advanced and reliable technology, large production scale, low energy consumption, standard tail gas, excellent comprehensive economic index and the like.
The double pressure method is characterized in that the ammoxidation pressure is 0.35 to 0.6MPa, and the ammonia absorption pressure is 1.0 to 1.5 MPa. The process flow has the following advantages:
1. low oxidation and absorption pressure and low device cost. 2. The oxidation rate of ammonia is up to more than 96%, the platinum consumption is low, and the platinum consumption is 120mg/t 100% nitric acid (before recovery). The nitrogen dioxide absorption rate is high, and the content of NOx in the discharged tail gas is less than 180 ppm. 3. The cold energy of ammonia evaporation is reasonably utilized, low-temperature cooling water with the temperature of 18 ℃ is prepared and sent to a cooling coil pipe of an absorption tower to remove the heat of absorption reaction, and the content of NOx gas in tail gas is effectively reduced. 4. The energy is fully recycled, and the economic benefit is obvious. The device can produce medium-pressure superheated steam (the pressure is 3.9MPa (G) and the temperature is about 440 ℃), can drive a steam turbine of a compressor unit and can also send the steam out, and the economic benefit is very obvious.
Air is fully mixed with ammonia gas through an ammonia-air mixer after being purified and compressed, the mixed ammonia-air mixed gas enters the top of an oxidation furnace and is uniformly distributed on a platinum net through a distributor to carry out catalytic oxidation reaction of the ammonia (4NH3+5O2 → 4NO +6H2O + Q) to release a large amount of heat, the reaction temperature is controlled to be about 860 ℃, NOx generated by reaction generates 3.9MPa (A) after heat exchange through a steam superheater and a waste heat boiler, superheated steam at 440 ℃ is supplied to a four-in-one unit steam turbine, and the surplus steam is sent into an outer pipe net and used for other devices in a plant area.
The oxidation furnace of the prior technical proposal generates medium-temperature and medium-pressure steam. For the steam turbine, if high-temperature high-pressure steam can be generated, the efficiency of the steam turbine is higher, the steam usage amount of the steam turbine is saved, and more high-temperature high-pressure steam with high quality is exported to create higher economic benefits for enterprises.
SUMMERY OF THE UTILITY MODEL
Aiming at the technical problem that the oxidation furnace can only generate medium-temperature and medium-pressure steam in the prior art. The utility model aims at providing a can produce nitric acid system of high temperature high pressure steam.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a nitric acid system capable of generating high-temperature and high-pressure steam comprises a steam turbine, wherein the steam turbine is connected with a steam drum through a condenser and an economizer in sequence, and the steam drum is connected with an oxidation furnace;
the condenser is used for condensing the steam turbine exhaust steam into condensed water and conveying the condensed water to the economizer, and the economizer is used for heating the condensed water into saturated water and conveying the heated saturated water into a steam drum;
the steam drum conveys the heated saturated water to the oxidation furnace for heating through a boiler water circulating pump, the saturated water is changed into supersaturated water and is conveyed back to the steam drum, and the steam drum is used for vaporizing the supersaturated water into saturated water and saturated steam and conveying the saturated water to the oxidation furnace through a pipeline;
the oxidation furnace is used for recovering heat released by ammonia oxidation reaction of air and ammonia, heating saturated water from the steam drum to be supersaturated water, heating saturated steam from the steam drum to be superheated steam, and outputting the supersaturated water and the superheated steam to the steam drum.
Further, a gas distributor, a platinum mesh plane, a pre-evaporation section, a superheating section and an evaporation section are sequentially arranged in the oxidation furnace along the axial direction, and the gas distributor is used for uniformly distributing air and gas-ammonia mixed gas fed from the outside to the platinum mesh plane to perform an ammoxidation reaction;
the pre-evaporation section, the overheating section and the evaporation section are used for heat exchange.
Further, the pre-evaporation section and the evaporation section are used for heating saturated water from the steam drum to be supersaturated water.
Specifically, the superheating section is used for heating saturated steam from the steam drum into superheated steam, so that high-temperature and high-pressure steam is generated and sent out.
Further, the pre-evaporation section comprises a 3-layer pre-evaporator coil group positioned at the top of the oxidation furnace and a water wall tube inside a lower shell of the oxidation furnace;
the superheating section comprises 5 layers of superheater coil groups positioned in the middle of the oxidation furnace;
the evaporation section comprises a 6-layer evaporator coil group positioned at the bottom of the oxidation furnace.
Further, a condensate pump, a deaerator and a boiler feed water pump are sequentially connected between the condenser and the economizer, and the condensate pump is used for conveying the condensate from the condenser to the deaerator for deaerating;
the boiler feed water pump is used for conveying the condensed water after oxygen removal to the economizer.
Further, steam separators for improving the cleanliness of superheated steam are arranged between the steam drum and the superheating section and between the steam drum and the steam turbine.
Furthermore, the bottom of the oxidation furnace is connected with the economizer through a tail gas reheater, and the tail gas reheater is used for reheating the tail gas from the oxidation furnace and sending the tail gas into the economizer.
Furthermore, the top of the oxidation furnace is connected with an ammonia-air mixer, and the ammonia-air mixer is used for mixing air and gas ammonia and conveying the mixture to the oxidation furnace.
Optionally, the steam drum is further connected with a decontamination tank.
Compared with the prior art, the utility model following beneficial effect has:
the utility model discloses an improve the steam quality of oxidation furnace product, reduce nitric acid manufacturing cost, increase the quality and the transport capacity of delivering steam outward simultaneously, further improve the economic benefits of enterprise.
Through optimizing the nitric acid device system, carry out reasonable performance matching to each equipment to fully recycle the heat that the ammoxidation released, make the oxidation furnace output high temperature high pressure superheated steam. Through improving the quality of steam, the high efficiency of performance steam turbine reduces the steam volume for the steam turbine, increases the defeated steam volume of outward conveying to greatly reduced the manufacturing cost of nitric acid product. Has the following advantages:
1. the energy released by the ammonia oxidation is fully recycled;
2. the device produces high-temperature high-pressure superheated steam (9.8MPa,540 ℃) as a byproduct, and improves the quality and the conveying capacity of the delivered steam besides driving a steam turbine of a compressor unit.
3. The steam turbine is driven by high-temperature high-pressure steam, so that the efficiency of the steam turbine is improved by about 3 percent;
4. the economic benefit of enterprises is improved, taking a nitric acid device producing 36 ten thousand tons every year as an example, the new process saves about 700 ten thousand of cost compared with the original process every year.
Drawings
FIG. 1 is a high temperature and high pressure steam system diagram of the present invention;
FIG. 2 is a schematic view of an oxidation oven according to the present invention;
the reference numerals in the figures denote:
01. a steam turbine; 02. a condenser; 03. a condensate pump; 04. a deaerator; 05. a boiler feed pump; 06. a coal economizer; 07. a steam drum; 08. a boiler water circulation pump; 09. an oxidation furnace; 091. a pre-evaporation section; 092. a superheating section; 093. an evaporation section; 10. an exhaust gas reheater; 11. a steam separator; 13. an ammonia superheater; 14. a gas ammonia filter; 15. an ammonia-air mixer; 16. an air filter; 17. an air compressor.
The present invention will be described in detail with reference to the drawings and the following detailed description.
Detailed Description
The following embodiments of the present invention are given, and it should be noted that the present invention is not limited to the following embodiments, and all the equivalent transformations made on the basis of the technical solution of the present application all fall into the protection scope of the present invention.
The present invention is described in detail with reference to the embodiments shown in the drawings, but it should be understood that these embodiments are not intended to limit the present invention, and those skilled in the art should understand that the functions, methods, or structural equivalents or substitutions made by these embodiments are within the scope of the present invention.
In the description of the present embodiments, it is to be understood that the terms "upper", "lower", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only used for convenience in describing the present invention and for simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
Example 1
Referring to fig. 1, the embodiment provides a nitric acid system capable of generating high-temperature and high-pressure steam, which comprises a steam turbine 01, wherein the steam turbine 01 is connected with a steam drum 07 through a condenser 02 and an economizer 06 in sequence, and the steam drum 07 is connected with an oxidation furnace 09;
the condenser 02 is used for condensing the steam turbine 01 exhaust into condensed water, so that a steam turbine exhaust port is established and kept in high vacuum and is conveyed to the economizer 06, and the economizer 06 is used for heating the condensed water into saturated water and sending the heated saturated water into the steam drum 07;
the steam drum 07 is used for conveying the heated saturated water to the oxidation furnace 09 through the boiler water circulating pump 08 to be heated to become supersaturated water and conveying the supersaturated water back to the steam drum 07, and the steam drum 07 is used for vaporizing the supersaturated water into saturated water and saturated steam and conveying the saturated water to the oxidation furnace 09 through a pipeline; the saturated water is continuously sent into the oxidation furnace 09 through the boiler water circulating pump 08 for circulating heating. The saturated steam in the vaporization enters the oxidation furnace 09 through a pipeline for further heating and becomes superheated steam. Therefore, the steam pocket 07 is not only an intersection point of the three processes of heating, vaporizing and overheating, but also a boundary point of the three processes of heating, vaporizing and overheating.
The oxidation furnace 09 recovers heat released by the ammoxidation of air and ammonia, heats saturated water from the steam drum 07 to supersaturated water, heats saturated steam from the steam drum 07 to superheated steam, and outputs the supersaturated water and the superheated steam to the steam drum 07.
Further, a gas distributor, a platinum mesh plane, a pre-evaporation section 091, a superheating section 092 and an evaporation section 093 are sequentially arranged in the oxidation furnace 09 along the axial direction, and the gas distributor is used for uniformly distributing air and gas ammonia mixed gas fed from the outside to the platinum mesh plane to perform an ammoxidation reaction;
the pre-evaporation section 091, the superheating section 092 and the evaporation section 093 are used for heat exchange.
Further, the boiler water circulation pump 08 delivers the saturated water in the steam drum 07 to the evaporation section coil of the oxidation furnace 09, and the evaporation section coil includes the pre-evaporation section 091 and the evaporation section 093, so that the pre-evaporation section 091 and the evaporation section 093 are used for heating the saturated water from the steam drum 07 to be supersaturated water. The supersaturated water returns to the steam drum 07 to be vaporized into saturated steam, and meanwhile, the separated saturated water is continuously conveyed into the oxidation furnace 09 through the boiler water circulating pump 08 to be subjected to heat exchange circulation;
specifically, the superheating section 092 is used for heating the saturated steam from the steam drum 07 into superheated steam, so as to realize delivery of high-temperature and high-pressure steam.
Further, the pre-evaporation section 091 comprises 3 layers of pre-evaporator coil groups positioned at the top of the oxidation furnace 09 and water wall tubes positioned inside the lower shell of the oxidation furnace 09; optionally, the water-cooled wall tube group is a plurality of circles of cooling wall tubes, and is arranged from the lower end socket to the straight section of the lower cylinder body, and inlet and outlet lead tubes of the wall tube group penetrate through the lower cylinder body and are connected to an inlet and outlet header of the evaporator outside the shell.
The superheating section 092 comprises a 5-layer superheater coil group located in the middle of the oxidation furnace 09; in order to obtain high-temperature superheated steam, the utility model discloses oxidation furnace 09 over heater coil area has been increased.
The evaporator section 093 includes a 6-layer evaporator coil set located at the bottom of the oxidation oven 09.
Further, a condensate pump 03, a deaerator 04 and a boiler feed water pump 05 are sequentially connected between the condenser 02 and the economizer 06, and the condensate pump 03 is used for conveying condensate from the condenser 02 to the deaerator 04 for deaerating; the deaerator 04 is used to remove oxygen and other gases in the desalted water and the condensed water of the steam turbine 01, which are input from the battery limits, and ensure the quality of the feed water. Meanwhile, the feed water can be heated to increase the feed water temperature of the oxidation furnace 09.
The boiler feed water pump 05 is used to deliver the deaerated condensed water to the economizer 06, and feed water having a sufficient pressure, flow rate, and equivalent temperature is continuously supplied to the economizer 06.
Further, steam separators 11 for improving the cleanliness of superheated steam are provided between the drum 07 and the superheating section 092 and between the drum 07 and the steam turbine 01. One stream of superheated steam from the oxidation furnace 09 enters a coil pipe inside the steam drum 07 through a three-way valve for heat exchange, a superheated steam pipeline after heat exchange is converged with a main superheated steam pipeline of the other stream of steam turbine 01 (steam turbine), and the temperature of the superheated steam is adjusted through flow.
Further, the bottom of the oxidation furnace 09 is connected with the economizer 06 through a tail gas reheater 10, and the tail gas reheater 10 is used for reheating the tail gas from the oxidation furnace 09 and sending the tail gas into the economizer 06.
Further, an ammonia air mixer 15 is connected to the top of the oxidation furnace 09, and the ammonia air mixer 15 is used for mixing and delivering air and ammonia to the oxidation furnace 09. As an example, the ammonia gas is connected with an ammonia empty mixer 15 through an ammonia superheater 13 and an ammonia filter 14, and the ammonia superheater 13 is used for heating the ammonia gas to reach the temperature required by the reaction. The gas ammonia filter 14 is used for further removing impurities in the gas ammonia and ensuring the activity of the platinum net of the ammoxidation catalyst.
In one embodiment, the air is connected to an air compressor 17 through an air filter 16, the air compressor 17 is connected to an ammonia air mixer 15, and the air filter 16 is used for purifying the air entering the air compressor 17 to ensure the safe operation of the air compressor 17. The air compressor 17 is used to raise the pressure and temperature required for the air to participate in the ammoxidation reaction.
Air is purified by an air filter 16 and then enters an air compressor 17 to be compressed, and the air pressure and the temperature are increased. The gas ammonia is heated by a gas ammonia superheater 13 and enters a gas ammonia filter 14 for purification. The air and the ammonia enter an ammonia-air mixer 15 to be mixed and then enter an oxidation furnace 09.
Optionally, the steam drum 07 is further connected to a decontamination tank, and discharges sewage to the decontamination tank.
To sum up, the nitric acid system capable of generating high-temperature and high-pressure steam has the following working conditions:
desalted water and steam turbine 01 (steam turbine) condensed water input in a boundary area are deoxidized through a deaerator 04 and then are conveyed to an economizer 06 through a high-pressure boiler water-feeding pump 05 (lift 1450m), boiler water is heated to 310 ℃ through further heat exchange in the economizer 06, the heated boiler water enters a steam drum 07, and the boiler water is conveyed to an oxidation furnace 09 through a boiler water circulating pump 08.
Saturated water from the steam drum 07 enters a pre-evaporator coil group and an evaporator coil group of the oxidation furnace 09 and exchanges heat with NOX reaction gas through the wall of the evaporator coil to convert the saturated water into supersaturated water, the supersaturated water returns to the steam drum to be flashed into steam after flowing out of a header of the evaporator, and the separated boiler water is continuously conveyed to the pre-evaporator and the evaporator coil group for heat exchange circulation through a boiler water circulating pump 08.
Saturated steam is conveyed to an oxidation furnace 09 superheater coil group through a pipeline, after the saturated steam from the steam pocket 07 enters the oxidation furnace 09 superheater coil group, heat exchange is carried out between the saturated steam and NOX reaction gas through the wall of the superheater coil group, the saturated steam is heated and converted into superheated steam, and a part of superheated steam coming out of the oxidation furnace 09 enters the coil pipe in the steam pocket 07 through a three-way valve to exchange heat and then is converged with another main superheated steam pipeline for adjusting the temperature of the superheated steam. The superheated steam after temperature adjustment directly enters a subsequent four-in-one unit to be used as the power of the unit. Because the system adopts high-temperature high-pressure steam, the efficiency of the steam turbine is greatly improved, and the steam consumption of the steam turbine is reduced. And the surplus large amount of superheated steam is output for other equipment.
The utility model discloses an oxidation furnace 09 explains:
the ammonia-air mixed gas from the ammonia-air mixer 15 enters from the top of the oxidation furnace 09, and the mixed gas is uniformly distributed on the plane of the platinum net after passing through the gas distributor in the oxidation furnace 09 and is subjected to chemical reaction at the platinum net to generate NOX reaction gas and release a large amount of heat. The NOX reaction gas downwards passes through the ceramic ring and the gas distribution plate and enters the pre-evaporator coil group, the evaporator coil group and the superheater coil group for heat exchange. The process gas temperature after heat exchange was 425 ℃.
With traditional medium temperature middling pressure steam nitric acid system with the utility model discloses a can produce nitric acid system process consumption index comparison (with 1 ton 100% NHO3 meter) of high temperature high pressure steam to 36 ten thousand tons of nitric acid device analog calculations of annual output are the example, and manufacturing cost 15 ~ 20 yuan can be practiced thrift to per ton nitric acid, then can practice thrift manufacturing cost about 700 ten thousand yuan every year. Has very good economic benefit.
The preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings, however, the present invention is not limited to the details of the above embodiments, and the technical concept of the present invention can be within the scope of the present invention to perform various simple modifications to the technical solution of the present invention, and these simple modifications all belong to the protection scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and in order to avoid unnecessary repetition, the present invention does not need to describe any combination of the features.
In addition, various embodiments of the present invention can be combined arbitrarily, and the disclosed content should be regarded as the present invention as long as it does not violate the idea of the present invention.
Claims (10)
1. A nitric acid system capable of generating high-temperature and high-pressure steam comprises a steam turbine (01) and is characterized in that the steam turbine (01) is connected with a steam drum (07) through a condenser (02) and an economizer (06) in sequence, and the steam drum (07) is connected with an oxidation furnace (09);
the condenser (02) is used for condensing the steam discharged by the steam turbine (01) into condensed water and conveying the condensed water to the economizer (06), and the economizer (06) is used for heating the condensed water to form saturated water and conveying the heated saturated water to the steam drum (07);
the steam drum (07) is used for conveying the heated saturated water to the oxidation furnace (09) through a boiler water circulating pump (08) to be heated to become supersaturated water and conveying the supersaturated water back to the steam drum (07), and the steam drum (07) is used for vaporizing the supersaturated water into saturated water and saturated steam and conveying the saturated water to the oxidation furnace (09) through a pipeline;
the oxidation furnace (09) is used for recovering heat released by the ammoxidation of air and ammonia gas, heating saturated water from the steam drum (07) to supersaturated water, heating saturated steam from the steam drum (07) to superheated steam, and outputting the supersaturated water and the superheated steam to the steam drum (07).
2. The nitric acid system capable of generating high-temperature and high-pressure steam as claimed in claim 1, wherein a gas distributor, a platinum mesh plane, a pre-evaporation section (091), a superheating section (092) and an evaporation section (093) are sequentially arranged in the oxidation furnace (09) along the axial direction, and the gas distributor is used for uniformly distributing the externally-fed air and gas ammonia mixed gas to the platinum mesh plane to perform an ammoxidation reaction;
the pre-evaporation section (091), the overheating section (092) and the evaporation section (093) are used for heat exchange.
3. A nitric acid system capable of generating high temperature and high pressure steam according to claim 2, wherein the pre-evaporation section (091) and the evaporation section (093) are used to heat the saturated water from the steam drum (07) to supersaturated water.
4. A nitric acid system capable of generating high-temperature high-pressure steam according to claim 2, wherein the superheating section (092) is used for heating saturated steam from the steam drum (07) into superheated steam to realize the outward sending of the high-temperature high-pressure steam.
5. A nitric acid system capable of generating high temperature and high pressure steam according to claim 2, wherein said pre-evaporation section (091) comprises 3 layers of pre-evaporator coil sets on top of the oxidation furnace (09) and water wall tubes inside the lower shell of the oxidation furnace (09);
the superheating section (092) comprises 5 layers of superheater coil groups positioned in the middle of the oxidation furnace (09);
the evaporator section (093) includes a 6-layer evaporator coil set located at the bottom of the oxidizer (09).
6. A nitric acid system capable of generating high-temperature and high-pressure steam according to claim 1, wherein a condensate pump (03), a deaerator (04) and a boiler feed pump (05) are connected between the condenser (02) and the economizer (06) in sequence, and the condensate pump (03) is used for conveying the condensate from the condenser (02) to the deaerator (04) for deaerating;
the boiler feed water pump (05) is used for conveying the condensed water after oxygen removal to the economizer (06).
7. A nitric acid system capable of producing high temperature and high pressure steam according to claim 2, wherein steam separators (11) for improving the cleanliness of superheated steam are provided between the steam drum (07) and the superheating section (092) and between the steam drum (07) and the steam turbine (01).
8. A nitric acid system capable of generating high-temperature high-pressure steam according to claim 1, wherein the bottom of the oxidation furnace (09) is connected with the economizer (06) through a tail gas reheater (10), and the tail gas reheater (10) is used for reheating the tail gas from the oxidation furnace (09) and sending the tail gas into the economizer (06).
9. A nitric acid system capable of generating high-temperature high-pressure steam according to claim 1, wherein the top of the oxidation furnace (09) is connected with an ammonia-air mixer (15), and the ammonia-air mixer (15) is used for mixing air and gas ammonia and delivering the mixture to the oxidation furnace (09).
10. A nitric acid system capable of generating high temperature and high pressure steam according to claim 1, wherein said steam drum (07) is further connected to a decontamination tank.
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