CN211659298U - Deacidification ammonia still - Google Patents
Deacidification ammonia still Download PDFInfo
- Publication number
- CN211659298U CN211659298U CN201922446971.XU CN201922446971U CN211659298U CN 211659298 U CN211659298 U CN 211659298U CN 201922446971 U CN201922446971 U CN 201922446971U CN 211659298 U CN211659298 U CN 211659298U
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- tower
- shaped liquid
- plate
- liquid baffle
- tray
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 27
- 239000007788 liquid Substances 0.000 claims abstract description 114
- 238000004821 distillation Methods 0.000 claims abstract description 14
- 239000000945 filler Substances 0.000 claims abstract description 5
- 238000012546 transfer Methods 0.000 abstract description 11
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 abstract description 7
- 235000011114 ammonium hydroxide Nutrition 0.000 abstract description 7
- 238000000926 separation method Methods 0.000 abstract description 4
- 239000007791 liquid phase Substances 0.000 description 7
- 238000012423 maintenance Methods 0.000 description 5
- 238000004939 coking Methods 0.000 description 4
- 230000007547 defect Effects 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 3
- 230000001174 ascending effect Effects 0.000 description 2
- 230000000712 assembly Effects 0.000 description 2
- 238000000429 assembly Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Abstract
The utility model discloses a deacidification ammonia still, which comprises a tower body, a tower tray and a filler section; at least two layers of tower trays are arranged in the lower part in the tower body in a vertically staggered manner; the tower tray comprises a tower tray plate, a down-flow plate, a liquid receiving tray, a V-shaped liquid baffle plate group, a connecting plate, a supporting beam, a supporting ring and a nozzle; the down-flow plate, the liquid receiving plate and the support ring are all fixed on the inner wall of the tower body; two arc edges of the tower plate are connected to the support ring; one of two straight sides of the tower plate is connected with the down-flow plate, and the other is connected with the liquid receiving plate; the supporting beam is fixed on the inner wall of the tower body; the nozzle is fixed on the tray plate through the supporting leg, and a bottom gap is formed between the nozzle and the tray plate; the tray plate is provided with air lifting holes, and the positions of the air lifting holes correspond to the nozzles; the V-shaped liquid baffle plate group is connected to the lower part of the tower tray plate through a connecting plate. The deacidification ammonia distillation tower meets the requirement of fluctuation and variation of parameters of a residual ammonia water system by changing the mass transfer form of gas and liquid in the tower, improves the separation efficiency of a tower tray, and reduces blockage.
Description
Technical Field
The utility model relates to a surplus aqueous ammonia distillation plant in chemical industry field specifically is a deacidification ammonia still.
Background
Currently, the deacidification ammonia still is mainly used for the separation and distillation process of residual ammonia water generated in the coking production process of a coking plant. In the process, the residual ammonia water is required to be firstly kept stand and separated in a raw material tank to be used as raw material ammonia water. And (3) heating the clarified raw material ammonia water to 96-98 ℃ in a heat exchanger, respectively entering a deacidification ammonia-distilling tower from the top and the middle upper part of the deacidification ammonia-distilling tower, extracting ammonia gas from a lateral line, and performing secondary condensation to finally obtain concentrated ammonia gas.
The deacidification ammonia still is used as the separation distillation equipment in the coking industry and mainly comprises a tower body and internal components. The internal components widely used in the deacidification ammonia distillation tower at present are a float valve tray or a vertical sieve tray. The main defects of the float valve tray are that the treatment capacity is small, the pressure drop is large, the blockage is easy, the float valve is easy to fall off, and the practical use effect of the deacidification ammonia still is not ideal. The main defects of the vertical sieve plate tower tray are that the mass transfer space is small, the gas-liquid entrainment is serious, the liquid extraction amount is small, and the small holes of the cap cover are easy to block and difficult to clean. The document with the application number of 200820143340.X discloses an anhydrous ammonia rectifying tower, which mainly comprises a tower body and a tray internal part, wherein the tray internal part is a vertical sieve plate type radial side guide jet tray, but the defect is that when waste water contains impurities, tar, dust and the like and is seriously blocked, the vertical sieve plate type radial side guide jet tray is used to cause serious blockage in the tower body due to the blockage of a cap cover, and the tower body is difficult to clean during maintenance; without a defoaming device, the gas-liquid is seriously entrained, so the practical effect is not good.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects of the prior art, the utility model aims to solve the technical problem of providing a deacidification ammonia-distilling tower.
The technical scheme of the utility model for solving the technical problems is that a deacidification ammonia distillation tower is provided, which comprises a tower body, a tower tray and a filler section; at least two layers of tower trays are arranged in the lower part in the tower body in a vertically staggered manner; the tower tray is characterized by comprising a tower tray plate, a down-flow plate, a liquid receiving tray, a V-shaped liquid baffle plate group, a connecting plate, a supporting beam, a supporting ring and a nozzle; the down-flow plate is fixed on the inner wall of the tower body, and the liquid receiving disc is fixed on the inner wall of the tower body; the support ring is fixed on the inner wall of the tower body; two arc edges of the tower plate are connected to the support ring; one of two straight sides of the tower plate is connected with the down-flow plate, and the other is connected with the liquid receiving plate; the supporting beam is fixed on the inner wall of the tower body and used for supporting the tray plate; the nozzle is fixed on the tray plate through the supporting legs, and a bottom gap is formed between the nozzle and the tray plate; the tray plate is provided with air lifting holes, and the positions of the air lifting holes correspond to the nozzles; the V-shaped liquid baffle plate group is connected to the lower part of the tower plate through a connecting plate;
the V-shaped liquid baffle plate group is divided into an upper layer V-shaped liquid baffle plate group and a lower layer V-shaped liquid baffle plate group in the vertical direction; a first gap is formed between the upper V-shaped liquid baffle plate group and the tower tray plate, and a second gap is formed between the upper V-shaped liquid baffle plate group and the lower V-shaped liquid baffle plate group; the upper layer V-shaped liquid baffle plate group is formed by parallel arrangement of n-1 horizontally placed V-shaped liquid baffle plates with downward openings, and the lower layer V-shaped liquid baffle plate group is formed by parallel arrangement of n horizontally placed V-shaped liquid baffle plates with downward openings; the V-shaped liquid baffle plates of the upper V-shaped liquid baffle plate group and the V-shaped liquid baffle plates of the lower V-shaped liquid baffle plate group are arranged in a staggered manner; the upper layer V-shaped liquid baffle plate group and the lower layer V-shaped liquid baffle plate group are symmetrically arranged at the center of the tower; the position of each V-shaped liquid baffle plate of the lower V-shaped liquid baffle plate group corresponds to the position of the air lifting holes, and the number of the V-shaped liquid baffle plates is the same as the row number of the air lifting holes; and in the same layer, a third gap is formed between every two adjacent V-shaped liquid baffle plates.
Compared with the prior art, the utility model discloses beneficial effect lies in:
(1) the tower tray used in the deacidification ammonia still is a tower tray with strong anti-blocking capability, large liquid lifting amount and small gas-liquid entrainment. Compared with a vertical sieve plate tower tray, the space between plates is almost a mass transfer space, the gas-liquid contact time is long, mass transfer is facilitated, and the mass transfer efficiency is higher; the V-shaped liquid baffle plate component separates liquid-phase entrainment, improves the mass transfer efficiency and prevents entrainment; the plate is not provided with easy-to-block parts, has strong anti-blocking capability and is suitable for treating an easy-to-foam system; the liquid lifting amount is higher, and the device is particularly suitable for systems with large liquid-gas ratio. The above advantages are all that vertical sieve tray can't realize, and to the more lagging float valve tray of technique, not only have above advantage, but also greatly reduced column plate quantity, extension maintenance cycle.
(2) The deacidification ammonia distillation tower can improve ammonia distillation efficiency, improve product quality, increase operation elasticity, save energy consumption and prolong maintenance period.
(3) This deacidification ammonia still utilizes neotype tower tray structural design through changing the interior gas-liquid mass transfer form of tower, can satisfy the fluctuating change requirement of parameter of surplus aqueous ammonia system, and the requirement of operation elasticity adaptation production more improves the separation efficiency of tower tray, reduces and blocks up, reduces the veneer pressure drop, makes product quality and production efficiency obviously promote, can be in the wide application of coking production. Tests show that the anti-blocking capability of the tower tray of the deacidification ammonia distillation tower can prolong the maintenance period by 50-100 percent compared with the maintenance period of the deacidification ammonia distillation tower in the prior art. When the number of the trays is the same, the treatment capacity of the trays of the deacidification ammonia distillation tower is increased by at least 20 percent compared with that of the deacidification ammonia distillation tower in the prior art, or the diameter of the designed tower is 100-200mm smaller than that of the traditional design, the structure is simple, and the cost is reduced.
(4) The deacidification ammonia distillation tower is suitable for newly-built projects and is also suitable for reconstruction of old towers, for example, the distance between trays (plates) is more than 350mm, the trays can be directly replaced, namely, the original float valve trays, vertical sieve plate trays or other trays are replaced by the tray plates and the assemblies (V-shaped liquid baffle plate assemblies, connecting plates and nozzles) on the plates, and a liquid descending system and a supporting system are unchanged, so that the applicability of industrial implementation is good.
Drawings
Fig. 1 is a schematic overall structure diagram of an embodiment of the present invention;
fig. 2 is a schematic front view of a tray according to an embodiment of the present invention;
fig. 3 is a schematic top view of a tray according to an embodiment of the present invention;
fig. 4 is a schematic cross-sectional view of the present invention along the direction a-a of fig. 3;
fig. 5 is a schematic view of an embodiment of the present invention.
In the figure: 1. a tower body; 2. a tray; 3. a filler section; 4. a tray plate; 5. a down-flow plate; 6. a liquid receiving plate; 7. a V-shaped liquid baffle plate group; 7-1, an upper V-shaped liquid baffle plate group; 7-2, a lower V-shaped liquid baffle plate group; 8. a connecting plate; 9. a support beam; 10. a support ring; 11. a nozzle; 12. and (4) air lifting holes.
Detailed Description
The present invention will be further explained with reference to the following embodiments and accompanying drawings. The specific embodiments are only used for further elaboration of the invention, and do not limit the scope of protection of the claims of the present application.
The utility model provides a deacidification ammonia still (see the figure 1-5), which comprises a tower body 1, a tower tray 2 and a filler section 3; the packing section 3 is positioned at the upper part inside the tower body 1, at least two layers of tower trays 2 are arranged at the lower part inside the tower body 1 in a vertically staggered manner, and a plate space is reserved between every two adjacent layers of tower trays 2;
the device is characterized in that the tray 2 comprises a tray plate 4, a down-flow plate 5, a liquid receiving tray 6, a V-shaped liquid baffle plate group 7, a connecting plate 8, a supporting beam 9, a supporting ring 10 and a nozzle 11; the down-flow plate 5 is vertically fixed on the inner wall of the tower body 1, and the liquid receiving plate 6 is welded and fixed on the inner wall of the tower body 1; the support ring 10 is welded and fixed on the inner wall of the tower body 1; two symmetrical arc edges of the tower plate 4 are connected to the support ring 10; one of two straight sides of the tower plate 4 is connected with the down-flow plate 5, and the other is connected with the liquid receiving plate 6; the liquid receiving plate 6 and the liquid descending plate 5 are respectively positioned on two sides of the tray plate 4; the supporting beam 9 is welded and fixed on the inner wall of the tower body 1, is positioned below the tray plate 4 and is used for supporting the tray plate 4; the nozzle 11 is welded and fixed on the tray plate 4 through the supporting legs, and a bottom gap is reserved between the nozzle 11 and the tray plate 4; the tray plate 4 is provided with an air lifting hole 12, the position of the air lifting hole 12 corresponds to the nozzle 11, and the nozzle 11 is in corresponding size fit with the air lifting hole 12 and is welded in a seamless manner; the V-shaped liquid baffle plate group 7 is welded with the lower part of the tower tray plate 4 through a connecting plate 8 and is positioned at the lower part of the tower tray plate 4;
the V-shaped liquid baffle plate group 7 is divided into an upper layer V-shaped liquid baffle plate group 7-1 and a lower layer V-shaped liquid baffle plate group 7-2 in the vertical direction; a first gap is formed between the upper V-shaped liquid baffle plate group 7-1 and the tower plate 4, and a second gap is formed between the upper V-shaped liquid baffle plate group 7-1 and the lower V-shaped liquid baffle plate group 7-2; the upper V-shaped liquid baffle plate group 7-1 is formed by arranging n-1 horizontally placed V-shaped liquid baffle plates with downward openings in parallel, and the lower V-shaped liquid baffle plate group 7-2 is formed by arranging n horizontally placed V-shaped liquid baffle plates with downward openings in parallel; the V-shaped liquid baffle plates of the upper V-shaped liquid baffle plate group 7-1 and the V-shaped liquid baffle plates of the lower V-shaped liquid baffle plate group 7-2 are arranged in a staggered manner; the upper layer V-shaped liquid baffle plate group 7-1 and the lower layer V-shaped liquid baffle plate group 7-2 are symmetrically arranged at the center of the tower respectively; the position of each V-shaped liquid baffle of the lower V-shaped liquid baffle group 7-2 corresponds to the position of the air lifting holes 12, and the number of the V-shaped liquid baffles is the same as the row number of the air lifting holes 12; in the same layer, a third gap is formed between every two adjacent V-shaped liquid baffle plates;
the air lifting hole 12 is an oblong hole; the size a of the bottom clearance is 8-15 mm; the size b of the first gap is 40-150 mm; the size c of the second gap is 50-150 mm; the size d of the third gap is determined according to the size of the air lifting hole 12 and the V-shaped liquid baffle plate;
the utility model discloses a theory of operation and work flow are: the liquid phase flows to the liquid receiving disc 6 of the upper layer from the liquid descending plate 5 side of the tray plate, when flowing through the tray plate 4, the liquid phase contacts with the ascending gas from the gas ascending hole 12 through the bottom gap between the nozzle 11 and the tray plate 4, the gas and the liquid contact forms a spraying state, and the liquid phase sprays to the plate space on the tray plate 4 for mass transfer, so that the gas and the liquid are fully contacted, and the mass transfer efficiency is improved; the gas phase carries the liquid phase to continuously rise and impacts a lower V-shaped liquid baffle plate group 7-2 below the upper layer of the tray plate 4; when the liquid collides with the V-shaped liquid baffle plate of the lower V-shaped liquid baffle plate group 7-2, the entrained liquid phase flows downwards along the same trend and falls back to the layer; and the liquid carried in the gas continuously rising from the third gap between the lower V-shaped liquid baffle plate group 7-2 collides with the V-shaped liquid baffle plate of the upper V-shaped liquid baffle plate group 7-1 and then flows downwards along the same direction, and then flows back to the layer along the outer side of the lower V-shaped liquid baffle plate group 7-2 to prevent entrainment. Thus, the gas phase and the liquid phase are separated quickly after mass transfer, thereby greatly improving the mass transfer efficiency.
The utility model discloses the nothing is mentioned the part and is applicable to prior art.
Claims (7)
1. A deacidification ammonia distillation tower comprises a tower body, a tower tray and a filler section; at least two layers of tower trays are arranged in the lower part in the tower body in a vertically staggered manner; the tower tray is characterized by comprising a tower tray plate, a down-flow plate, a liquid receiving tray, a V-shaped liquid baffle plate group, a connecting plate, a supporting beam, a supporting ring and a nozzle; the down-flow plate is fixed on the inner wall of the tower body, and the liquid receiving disc is fixed on the inner wall of the tower body; the support ring is fixed on the inner wall of the tower body; two arc edges of the tower plate are connected to the support ring; one of two straight sides of the tower plate is connected with the down-flow plate, and the other is connected with the liquid receiving plate; the supporting beam is fixed on the inner wall of the tower body and used for supporting the tray plate; the nozzle is fixed on the tray plate through the supporting legs, and a bottom gap is formed between the nozzle and the tray plate; the tray plate is provided with air lifting holes, and the positions of the air lifting holes correspond to the nozzles; the V-shaped liquid baffle plate group is connected to the lower part of the tower plate through a connecting plate;
the V-shaped liquid baffle plate group is divided into an upper layer V-shaped liquid baffle plate group and a lower layer V-shaped liquid baffle plate group in the vertical direction; a first gap is formed between the upper V-shaped liquid baffle plate group and the tower tray plate, and a second gap is formed between the upper V-shaped liquid baffle plate group and the lower V-shaped liquid baffle plate group; the upper layer V-shaped liquid baffle plate group is formed by parallel arrangement of n-1 horizontally placed V-shaped liquid baffle plates with downward openings, and the lower layer V-shaped liquid baffle plate group is formed by parallel arrangement of n horizontally placed V-shaped liquid baffle plates with downward openings; the V-shaped liquid baffle plates of the upper V-shaped liquid baffle plate group and the V-shaped liquid baffle plates of the lower V-shaped liquid baffle plate group are arranged in a staggered manner; the upper layer V-shaped liquid baffle plate group and the lower layer V-shaped liquid baffle plate group are symmetrically arranged at the center of the tower; the position of each V-shaped liquid baffle plate of the lower V-shaped liquid baffle plate group corresponds to the position of the air lifting holes, and the number of the V-shaped liquid baffle plates is the same as the row number of the air lifting holes; and in the same layer, a third gap is formed between every two adjacent V-shaped liquid baffle plates.
2. The deacidification ammonia still according to claim 1, wherein the number of each V-shaped liquid baffle plate of the lower V-shaped liquid baffle plate group is the same as the row number of the gas lifting holes.
3. The deacidification ammonia still according to claim 1, wherein the gas lift holes are oblong holes.
4. The deacidification ammonia still according to claim 1, wherein the size of the bottom gap a is 8-15 mm.
5. The deacidification ammonia still according to claim 1, wherein the size b of the first gap is 40-150 mm.
6. The deacidification ammonia still according to claim 1, wherein the size c of the second gap is 50-150 mm.
7. The deacidification ammonia still according to claim 1, wherein the size d of the third gap is determined according to the size of the lift vent and the V-baffle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922446971.XU CN211659298U (en) | 2019-12-30 | 2019-12-30 | Deacidification ammonia still |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922446971.XU CN211659298U (en) | 2019-12-30 | 2019-12-30 | Deacidification ammonia still |
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| Publication Number | Publication Date |
|---|---|
| CN211659298U true CN211659298U (en) | 2020-10-13 |
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|---|---|---|---|
| CN201922446971.XU Active CN211659298U (en) | 2019-12-30 | 2019-12-30 | Deacidification ammonia still |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR102662139B1 (en) * | 2023-11-13 | 2024-05-02 | 덕산실업(주) | Purification method and purification apparatus of nmp |
-
2019
- 2019-12-30 CN CN201922446971.XU patent/CN211659298U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR102662139B1 (en) * | 2023-11-13 | 2024-05-02 | 덕산실업(주) | Purification method and purification apparatus of nmp |
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