CN211619953U - Production system of sodium nitrate and sodium nitrite - Google Patents
Production system of sodium nitrate and sodium nitrite Download PDFInfo
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- CN211619953U CN211619953U CN201922444719.5U CN201922444719U CN211619953U CN 211619953 U CN211619953 U CN 211619953U CN 201922444719 U CN201922444719 U CN 201922444719U CN 211619953 U CN211619953 U CN 211619953U
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Abstract
The utility model provides a production system of sodium nitrate and sodium nitrite, including nitric oxide production unit, neutralization liquid production unit, sodium nitrate production unit and the sodium nitrite production unit that communicates in proper order, neutralization liquid production unit includes the alkali absorption tower, the alkali absorption tower includes the body of the tower, the body of the tower bottom is equipped with gas distributor, and the top is equipped with liquid distributor, be equipped with multistage absorption unit along highly being equipped with between liquid distributor and the gas distributor, every grade absorption unit all includes the column plate and arranges the filler district of column plate below in, the column plate package rubbing board body, evenly open on the plate body has a plurality of blanking holes, every blanking hole edge downwardly extending gathers material portion, and gathers material portion bottom and open there is the opening. The utility model discloses a be equipped with the column plate of the alkali absorption tower of gathering material portion, assemble the liquid drop on the column plate after along gathering the opening of material portion and flow down, avoid the solution of packing portion to distribute unevenly.
Description
Technical Field
The utility model belongs to the chemical production field especially relates to a production system of sodium nitrate and sodium nitrite.
Background
Sodium nitrate and sodium nitrite are important intermediate raw materials in the industries of medicine, glass, dye and civil explosion, and the prior factory usually produces the sodium nitrate and the sodium nitrite by a concentrated gas method, wherein the method is to directly absorb nitrogen oxide gas from an independent ammonia oxidation system by sodium carbonate alkali liquor, and then produce sodium nitrite and sodium nitrate products by the processes of evaporation, crystallization and the like, so that the large-scale continuous production of the sodium nitrate and the sodium nitrite can be realized, and the productivity is ensured. However, the absorption rate of the nitric oxide gas is low in the production process, so that the product purity is low, the product value is influenced, and the subsequent production of sodium nitrate and sodium nitrite is difficult.
SUMMERY OF THE UTILITY MODEL
In view of this, the present invention is directed to a system for producing sodium nitrate and sodium nitrite to improve the absorption rate of nitrogen oxide gas.
In order to achieve the above purpose, the technical scheme of the utility model is realized like this:
a production system of sodium nitrate and sodium nitrite comprises
The device comprises a nitric oxide production unit, a neutralization solution production unit, a sodium nitrate production unit and a sodium nitrite production unit which are sequentially communicated, wherein the neutralization solution production unit comprises an alkali absorption tower, the alkali absorption tower comprises a tower body, a gas distributor is arranged at the bottom of the tower body, a liquid distributor is arranged at the top of the tower body, a multi-stage absorption unit is arranged between the liquid distributor and the gas distributor along the height, each stage of absorption unit comprises a tower plate and a packing area arranged below the tower plate, the tower plate comprises a plate body, a plurality of blanking holes are uniformly formed in the plate body, each blanking hole edge extends downwards to form a material gathering part, and the bottom end of the material gathering part is provided with an opening.
Further, the material gathering part is conical, and the opening is formed in the bottom end of the material gathering part.
Further, the diameter of the tower body is gradually increased upwards along the vertical direction.
Further, the sodium nitrite production unit includes first heat transfer device and the first crystallizer of establishing ties in proper order, first heat transfer device includes one-level evaporimeter, second grade evaporimeter and the tertiary evaporimeter of establishing ties each other, the liquid outlet after the first crystallizer includes concentrate import and centrifugation, the concentrated solution import intercommunication of the tube side of tertiary evaporimeter and first crystallizer.
Further, the sodium nitrate production unit includes second heat transfer device and the second crystallizer of establishing ties in proper order, second heat transfer device includes one-level evaporimeter, second grade evaporimeter and the tertiary evaporimeter of establishing ties each other, the second crystallizer includes the concentrated solution import and the liquid outlet after the centrifugation, the tube side of tertiary evaporimeter and the concentrated solution import intercommunication of second crystallizer.
Further, the nitrogen oxide production unit comprises a gas mixer and an oxidation furnace which are communicated with each other, wherein a gas outlet of the gas mixer is communicated with a gas inlet of the oxidation furnace.
Furthermore, a waste heat boiler is arranged between the nitrogen oxide production unit and the neutralization solution production unit, the waste heat boiler comprises a boiler air inlet, a boiler air outlet, a desalted water inlet and a steam outlet, the air outlet of the oxidation furnace is communicated with the boiler air inlet, and the boiler air outlet is communicated with a gas distributor of the alkali absorption tower.
Furthermore, a condensate heating pipe is arranged on the periphery of a concentrated solution inlet of the first crystallizer, and the condensate heating pipe is communicated with the shell sides of the first-stage evaporator, the second-stage evaporator and the third-stage evaporator.
Furthermore, a condensate heating pipe is arranged on the periphery of a concentrated solution inlet of the second crystallizer and is communicated with the shell sides of the first-stage evaporator, the second-stage evaporator and the third-stage evaporator.
Compared with the prior art, the production system of sodium nitrate and sodium nitrite of the utility model has the following advantages:
the utility model adopts the tower plate of the alkali absorption tower provided with the material gathering part, and liquid drops on the tower plate flow down along the opening of the material gathering part after gathering, thereby avoiding the uneven distribution of the solution in the filling part;
the diameter-variable tower body is adopted so as to control the pressure in the tower.
The first-stage evaporator, the second-stage evaporator and the third-stage evaporator are connected in series, so that steam is recycled, and the use efficiency of the steam is improved;
a condensate heating pipe is arranged at a concentrated solution inlet of the crystallizer, and the temperature of the condensate condensed by steam is utilized to keep the temperature of the concentrated solution inlet, so that the concentrated solution is prevented from crystallizing in a pipeline to cause pipeline blockage.
Drawings
The accompanying drawings, which form a part hereof, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without undue limitation. In the drawings:
FIG. 1 is a schematic view of the production system as a whole;
FIG. 2 is a schematic view of a waste heat boiler;
FIG. 3 is a schematic diagram of a crystallizer;
FIG. 4 is a schematic view of an alkali absorption column.
Description of reference numerals:
1-a nitrogen oxide production unit; 11-a gas mixer; 12-an oxidation furnace; 13-a waste heat boiler; 131-a boiler inlet; 132-boiler outlet; 133-desalted water inlet; 134-a steam outlet; 2-a neutralization solution production unit; 21-an alkali absorber column; 211-a tower body; 212-a gas distributor; 2121-nitric oxide inlet; 213-a liquid distributor; 2131-alkali liquor inlet; 214-an absorption unit; 2141-a column plate; 21411-a plate body; 21412-blanking holes; 21413-a polymer section; 21414-an opening; 2142-a filler region; 215-outlet for neutralization solution; a 3-sodium nitrite production unit; 31-first heat exchange means; 311-first stage evaporator; 312-a secondary evaporator; 313-a three-stage evaporator; 32-a first crystallizer; 321-a concentrated solution inlet; 322-a centrifuged liquid outlet; 323-condensate heating pipe; 4-sodium nitrate production unit; 41-second heat exchange means; 42-a second crystallizer; 5-steam condenser.
Detailed Description
It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are used merely for convenience of description and for simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
As shown in fig. 1, the production system of sodium nitrate and sodium nitrite of the present invention comprises a nitric oxide production unit 1, a neutralization solution production unit 2, a sodium nitrite production unit 3 and a sodium nitrate production unit 4 which are connected in series in sequence, wherein the nitric oxide production unit 1 comprises a gas mixer 11 and an oxidation furnace 12, ammonia gas and air are conveyed into the gas mixer 11, the two gases are fully mixed by the gas mixer 11, the gas outlet of the gas mixer 11 is communicated with the gas inlet of the oxidation furnace 12, and the air and the ammonia gas are oxidized and reacted by the oxidation furnace 12 to generate NOX; .
As shown in fig. 2, a waste heat boiler 13 is disposed between the nitrogen oxide production unit 1 and the neutralization solution production unit 2, the waste heat boiler 13 includes a boiler inlet 131, a boiler outlet 132, a desalted water inlet 133, and a steam outlet 134, the outlet of the oxidation furnace 12 is communicated with the boiler inlet 131, NOX generated from the oxidation furnace 12 is introduced into the boiler inlet 131 so that the NOX flows through the waste heat boiler 13 and is discharged from the boiler outlet 132, and simultaneously, desalted water is introduced into the desalted water inlet 133, and the desalted water is heated by the heat of the nitrogen oxide gas so that the desalted water is superheated and evaporated into steam, and the steam is discharged from the steam outlet 134 out of the waste heat boiler 13.
Referring to fig. 4, the neutralization liquid production unit 2 includes a plurality of alkali absorption towers 21 connected in series or in parallel, each alkali absorption tower 21 includes a tower body 211, the diameter of the bottom of the tower body 211 is larger than that of the top of the tower body, the diameter of the tower body is gradually increased upwards along the vertical direction, a gas distributor 212 is disposed at the bottom of the tower body 211, a liquid distributor 213 is disposed at the top of the tower body, a plurality of stages of absorption units 214 (only one stage of absorption unit 214 is shown in the drawing for simplifying the structure) are disposed between the liquid distributor 213 and the gas distributor 212 along the height, each stage of absorption unit 214 includes a tower plate 2141 and a filler region 2142 disposed below the tower plate 2141, how to dispose the filler in the filler region 2142 and the type of the filler are the prior art, and will not be described again herein; in the original tower plate 2141 structure, when the temperature in the alkali absorption tower 21 is high during the operation of the alkali absorption tower 21, the alkali liquid is evaporated, which causes the concentration of the alkali liquid to increase and condense into liquid drops on the tower plate 2141, which drop downwards, and will affect the concentration of the alkali liquid on the packing, which is not beneficial to the reaction of nitrogen oxide and the alkali liquid, the tower plate 2141 used in the present invention comprises a plate body 21411, a plurality of blanking holes 21412 are uniformly opened on the plate body 21411, a conical material gathering part 21413 extends downwards from the edge of each blanking hole 21412, and an opening 21414 is opened at the tip of the conical material gathering part 21413, the liquid beads condensed on the tower plate 2141 during the operation can flow downwards along the material gathering part 21413 until the liquid beads flow to the opening 21414, which flows down along with the alkali liquid, so that the liquid condensed by steam flows down after being mixed with the alkali liquid, which reduces the influence of the liquid drops on the reaction, accelerates the reaction efficiency, and during the operation of the alkali absorption tower 21, introducing air into the alkali absorption tower 21, changing the air pressure in the alkali absorption tower 21, keeping the micro-positive pressure in the alkali absorption tower 21 so as to facilitate the reaction of alkali liquor and nitric oxide gas, and controlling the proportion of nitrate radicals and nitrite radicals; and the boiler outlet 132 of the waste heat boiler 13 is communicated with the gas distributor 212 of the alkali absorption tower 21
The top of the alkali absorption tower 21 is provided with an alkali liquor inlet 2131, the bottom of the alkali absorption tower 21 is provided with a neutralization solution outlet 215 and a nitric oxide inlet 2121, the NOX gas enters the alkali absorption tower 21 along the nitric oxide inlet 2121 and moves upwards, the alkali liquor enters the alkali absorption tower 21 along the alkali liquor inlet 2131 and moves downwards, so that the alkali liquor and the nitric oxide gas undergo neutralization reaction at an absorption unit 214 in the alkali absorption tower 21 to generate sodium nitrite and sodium nitrate solution, and then the sodium nitrite and sodium nitrate solution fall to the bottom of the alkali absorption tower 21 and are discharged out of the alkali absorption tower 21 through the neutralization solution outlet 215.
Referring to fig. 3, the sodium nitrite production unit 3 includes a first heat exchange device 31 and a first crystallizer 32 connected in series; the sodium nitrate production unit 4 comprises a second heat exchange device 41 and a second crystallizer 42 which are sequentially connected in series, and a conversion mechanism is connected in series between the sodium nitrite production unit 3 and the sodium nitrate production unit 4;
the first heat exchange device 31 and the second heat exchange device 41 respectively comprise a first-stage evaporator 311, a second-stage evaporator 312 and a third-stage evaporator 313 which are sequentially connected in series, the neutralization liquid sequentially enters tube passes of the first-stage evaporator 311, the second-stage evaporator 312 and the third-stage evaporator 313 of the first heat exchange device 31, the steam generated in the waste heat boiler 13 passes through the shell passes of the first-stage evaporator 311, the second-stage evaporator 312 and the third-stage evaporator 313 in sequence, the neutralized liquid is heated by the steam, and the temperature of the nitrogen oxide gas generated in the oxidation furnace 12 is about 200 deg., the desalted water is heated by the nitrogen oxide gas, so that the desalted water is evaporated into high-temperature steam, the high-temperature steam is introduced into the shell passes of the first heat exchange device 31 and the second heat exchange device 41, concentrating the solution in the tube pass of the first heat exchange device 31 and the second heat exchange device 41 to form a concentrated solution, so that the first crystallizer 32 and the second crystallizer 42 carry out centrifugal crystallization on the solution;
the first crystallizer 32 and the second crystallizer 42 both comprise a concentrated solution inlet 321 and a centrifuged solution outlet 322, the concentrated solution is added into the first crystallizer 32 and then cooled and crystallized, sodium nitrite crystals are obtained in the first crystallizer 32, sodium nitrate crystals are obtained in the second crystallizer 42, the centrifuged solution outlet 322 of the first crystallizer 32 is communicated with the conversion mechanism, so that the centrifuged solution enters the conversion mechanism, at the moment, the centrifuged solution is a mixed solution containing sodium nitrate and a small amount of sodium nitrite, dilute nitric acid and air are added into the conversion mechanism, the sodium nitrite, the dilute nitric acid and the air react to obtain a 2NaNO2+2HNO3 ═ 2NaNO3+ NO × + NO ≧ 2 × + H2O, the sodium nitrate solution is prepared into a sodium nitrate solution, the reacted sodium nitrate solution is obtained, the conversion mechanism is communicated with the second heat exchange device 41, the sodium nitrate solution is heated, and concentrated and processed, and adding the concentrated solution of the sodium nitrate solution into the second crystallizer 42, and crystallizing through the second crystallizer 42 to obtain sodium nitrate crystals, wherein the specific structure and the using method of the conversion mechanism are the prior art, and are not described herein again.
The peripheral sides of the concentrated solution inlets 321 of the first crystallizer 32 and the second crystallizer 42 are provided with condensed solution heating pipes 323, the condensed solution heating pipes 323 are communicated with the shell passes of the first-stage evaporator 311, the second-stage evaporator 312 and the third-stage evaporator 313, and the concentrated solution inlets 321 are heated by using condensed solutions generated by the first heat exchanger and the second heat exchanger after heat exchange, so that the concentrated solution is prevented from crystallizing in a pipeline and causing pipeline blockage.
In particular, the first crystallizer 32 and the second crystallizer 42 are OSLO crystallizers.
The low-temperature steam discharged from the three-stage evaporator 313, the first crystallizer 32 and the second crystallizer 42 is respectively introduced into a tube pass of a steam condenser 5, and circulating water is introduced into a shell pass of the steam condenser 5, so that the steam is cooled and condensed.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (9)
1. A production system of sodium nitrate and sodium nitrite which is characterized in that: a nitric oxide production unit (1), a neutralizing solution production unit (2), a sodium nitrite production unit (3) and a sodium nitrate production unit (4) which are communicated in sequence, the neutralization solution production unit (2) comprises an alkali absorption tower (21), the alkali absorption tower (21) comprises a tower body (211), the bottom of the tower body (211) is provided with a gas distributor (212), the top is provided with a liquid distributor (213), a plurality of absorption units (214) are arranged between the liquid distributor (213) and the gas distributor (212) along the height, each absorption unit (214) comprises a tower plate (2141) and a packing area (2142) arranged below the tower plate (2141), the tower plate (2141) comprises a plate body (21411), a plurality of blanking holes (21412) are uniformly formed in the plate body (21411), a material gathering portion (21413) extends downwards from the edge of each blanking hole (21412), and an opening (21414) is formed in the bottom end of the material gathering portion (21413).
2. The system for producing sodium nitrate and sodium nitrite according to claim 1, wherein: the material gathering part (21413) is conical, and the opening (21414) is formed at the bottom end thereof.
3. The system for producing sodium nitrate and sodium nitrite according to claim 1, wherein: the diameter of the tower body (211) is gradually increased upwards along the vertical direction.
4. The system for producing sodium nitrate and sodium nitrite according to claim 1, wherein: sodium nitrite production unit (3) are including first heat transfer device (31) and first crystallizer (32) of establishing ties in proper order, first heat transfer device (31) are including one-level evaporimeter (311), second grade evaporimeter (312) and tertiary evaporimeter (313) of establishing ties each other, liquid outlet (322) after first crystallizer (32) include concentrate import (321) and the centrifugation, the tube side of tertiary evaporimeter (313) and concentrate import (321) the intercommunication of first crystallizer (32).
5. The system for producing sodium nitrate and sodium nitrite according to claim 1, wherein: sodium nitrate production unit (4) are including second heat transfer device (41) and second crystallizer (42) that establish ties in proper order, second heat transfer device (41) are including one-level evaporimeter (311), second grade evaporimeter (312) and tertiary evaporimeter (313) that establish ties each other, second crystallizer (42) are including concentrate import (321) and centrifugation back liquid outlet (322), the tube side of tertiary evaporimeter (313) communicates with concentrate import (321) of second crystallizer (42).
6. The system for producing sodium nitrate and sodium nitrite according to claim 1, wherein: the nitric oxide production unit (1) comprises a gas mixer (11) and an oxidation furnace (12) which are communicated with each other, wherein a gas outlet of the gas mixer (11) is communicated with a gas inlet of the oxidation furnace (12).
7. The system for producing sodium nitrate and sodium nitrite as claimed in claim 6, wherein: be equipped with a waste heat boiler (13) between nitrogen oxide production unit (1) and neutralization solution production unit (2), waste heat boiler (13) are including boiler air inlet (131), boiler gas outlet (132), demineralized water entry (133) and steam outlet (134), the gas outlet and boiler air inlet (131) intercommunication of oxidation furnace (12), gas distributor (212) intercommunication of boiler gas outlet (132) and alkali absorption tower (21).
8. The system for producing sodium nitrate and sodium nitrite as claimed in claim 4, wherein: and a condensate heating pipe (323) is arranged on the periphery of a concentrated solution inlet (321) of the first crystallizer (32), and the condensate heating pipe (323) is communicated with the shell sides of the primary evaporator (311), the secondary evaporator (312) and the tertiary evaporator (313).
9. The system for producing sodium nitrate and sodium nitrite as claimed in claim 5, wherein: and a condensate heating pipe (323) is arranged on the peripheral side of a concentrated solution inlet (321) of the second crystallizer (42), and the condensate heating pipe (323) is communicated with the shell sides of the primary evaporator, the secondary evaporator (312) and the tertiary evaporator (313).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201922444719.5U CN211619953U (en) | 2019-12-27 | 2019-12-27 | Production system of sodium nitrate and sodium nitrite |
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| CN201922444719.5U CN211619953U (en) | 2019-12-27 | 2019-12-27 | Production system of sodium nitrate and sodium nitrite |
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| CN211619953U true CN211619953U (en) | 2020-10-02 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114735725A (en) * | 2022-05-07 | 2022-07-12 | 山东海化集团有限公司 | Method for preparing neutralization solution in sodium sulfate production process |
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2019
- 2019-12-27 CN CN201922444719.5U patent/CN211619953U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114735725A (en) * | 2022-05-07 | 2022-07-12 | 山东海化集团有限公司 | Method for preparing neutralization solution in sodium sulfate production process |
| CN114735725B (en) * | 2022-05-07 | 2023-05-16 | 山东海化集团有限公司 | Method for preparing neutralization solution in production process of disodium |
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Address after: 2-504, Beichen building, southwest of the intersection of Beijing Tianjin highway and Longzhou Road, BeiCang Town, Beichen District, Tianjin Patentee after: Tianjin Huajing Engineering Technology Co.,Ltd. Address before: 2-504, Beichen building, southwest of the intersection of Beijing Tianjin highway and Longzhou Road, BeiCang Town, Beichen District, Tianjin Patentee before: TIANJIN HUAJING CHEMICAL ENGINEERING NEW TECHNOLOGY DEVELOPMENT Co.,Ltd. |