CN1215620A - Plate tower for mass-transfer process with thermal reaction - Google Patents
Plate tower for mass-transfer process with thermal reaction Download PDFInfo
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- CN1215620A CN1215620A CN 97107740 CN97107740A CN1215620A CN 1215620 A CN1215620 A CN 1215620A CN 97107740 CN97107740 CN 97107740 CN 97107740 A CN97107740 A CN 97107740A CN 1215620 A CN1215620 A CN 1215620A
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Abstract
A plate-type tower used for the mass transfer process having thermal reaction is an absorptive cleaning tower especially suitable for the mass transfer process having small quantity of exthothermal reaction, such as carbonizing and comprehensive ammonia recovery cleaning tower, escaped synthetic gas recovery tower and synthetic gases recovery tower in chemical fertilizer industry. Its structure features especially designed raised gas concentrating tower tray, cooling balance zone tower tray and foam-removing zone, use of vertical sieve tray as main mass transfer tower tray, and alternative arranged cooling balance zone tower trays and main mass transfer tower trays. Its advantages are high mass transfer efficiency, high throughout of gas, low contents of NH3 and CO2 in discharged gas,and less consumption of soft water.
Description
The present invention relates to a kind of plate column of mass-transfer process with thermal reaction, particularly relate to the plate column that mass transport process has a small amount of exothermic reaction, reclaim as the comprehensive ammonia of the carbonization in the fertilizer industry and clean tower, the synthetic recovery tower of exitting of speeding, and synthetic two gas recovery towers.
At fertilizer industry, medium and small nitrogen fertilizer factory particularly, the comprehensive ammonia of carbonization that uses in producing at present reclaims and cleans tower, and the synthetic recovery tower of speeding to exit, synthetic two gas recovery towers mostly are the bubble column of traditional structure greatly.Plate column is cleaned in the recovery of this structure, although still be extensive use of at present, the place of its deficiency also is that the present technique field is in common knowledge.Here it is, and mass-transfer efficiency is low, and structure is complicated, keeps in repair very difficultly, and equipment easily stops up, and carbonization tail gas runs height often.Run height in order to overcome tail gas, the normal method that strengthens the soft water injection rate that adopts in the production, this has caused a large amount of weak aqua ammonias to produce again.Unserviceable weak aqua ammonia normally enters trench, and this is contaminated environment both, causes the waste of ammonia and soft water again.In order to improve this situation in the nitrogen fertilizer production, people have carried out exploring widely.Development zone, the Shijiazhuang efficient tower of positive element company is used for little nitrogen fertilizer production with the vertical sieve tray technology, the tower tray of having developed whole tower all is that tower is cleaned in the recovery of vertical sieve tray tower tray, and applied for Chinese utility model patent, in the power of patenting on March 16th, 1993 (patent No. is ZL92232700.9).The vertical sieve tray tower tray is made of sieve plate and the bubble-cap that is positioned at the sieve aperture top, is processed with the passage vertical with sieve aperture on the bubble-cap wall.This tower tray belongs to the ejection-type column plate, and mass-transfer efficiency is very high.But in nitrogen fertilizer production, the absorption process that synthesis gas is dissolved in water is exothermic reaction, and water-soluble mass transfer rate raises along with water temperature and reduces.This patent is not noticed this problem, takes corresponding technical measures.Thereby the carbonization comprehensive tower that is used for little nitrogen fertilizer production of the efficient tower of positive element company exploitation, in producing summer, particularly in producing the summer of southern area, because the temperature water temperature is higher and the exothermic reaction of dissolving in the absorption process, the tower body temperature raises, and result of use is not good, the NH in the tail gas
3Gas, CO
2Gas is all above national standard.Enterprise produces needs in order to satisfy, a large amount of soft water of annotating of still having to, and a large amount of unserviceable weak aqua ammonia discharging trenches, production cost and energy consumption are higher, and also carry a large amount of liquid foams in the tail gas secretly.Therefore, in production practices, have minority nitrogen fertilizer plant to adopt this tower after, be far from reaching designing requirement, the factory that has even abandon this tower seeks new technology in addition.
At the deficiency of above-mentioned prior art, the object of the present invention is to provide a kind ofly in mass transport process, heat exchange is carried out on mass transfer limit, limit, the mass-transfer efficiency height, energy consumption and production cost are low, and gas processing capability is big, and pressure drop is low, and plate column is cleaned in not susceptible to plugging absorption.
Can realize the absorption cleaning plate column of the object of the invention, include tower body, tower tray, gas inlet and outlet, liquid entrance, and on one deck tower tray column plate, being provided for cooling off or heating the heat-exchanger rig of absorption liquid at least, the column plate that the tower tray layer of heat-exchanger rig is set is a sieve plate.
In order to realize purpose of the present invention better, the present invention has also taked following technical measures:
The tower tray layer that heat-exchanger rig is not set adopts the vertical sieve tray tower tray.The structure of vertical sieve tray tower tray can be designed to be made of sieve plate column plate and the bubble-cap that is arranged on sieve aperture top, is processed with the passage vertical with sieve aperture on the bubble-cap wall, and the bead face of bubble-cap is parallel with the sieve plate face and certain interval arranged.
The basecoat tower tray of tower concentrates tower tray for the calotte formula rises gas, rises inflator with the list that replaces prior art and rises the gas section.The calotte formula rises structure that gas concentrates tower tray and can be designed to by column plate, be installed with rising inflator, constitute with the calotte and the drain pipe that rise the inflator phase configuration on column plate, and calotte is arranged on and rises above the inflator, is processed with the bar shaped passage on the calotte wall.
The place that is no less than 0.5 meter above the last layer tower tray of tower is provided with Despumation device, removes the liquid of carrying secretly in the gas.
The tower tray of heat-exchanger rig is set, and its neighbouring tower tray is not for being provided with the tower tray of heat-exchanger rig.When the tower tray layer that heat-exchanger rig is set is no less than 2, be positioned at tower top be provided with heat-exchanger rig tower tray its tower tray number of plies of heat-exchanger rig is not set up and down, greater than be positioned at the tower bottom be provided with heat-exchanger rig tower tray its tower tray number of plies of heat-exchanger rig is not set up and down.
Heat-exchanger rig is the heat exchanger tube axis horizontal heat exchanger parallel with the sieve plate face, and the height of heat exchanger tube is not more than the height of tower tray downflow weir.Preferably horizontal heat-exchanger rig is designed to the bend pipe drawer-type structure, and two separate bend pipe drawer type heat-exchanger rigs are set on a tower tray.
The present invention takes abovementioned technology to have following relatively more outstanding advantageous effect:
1. the distinctive cooling balancing segment of the present invention promptly is provided with the tower tray section of heat-exchanger rig on the sieve plate column plate, not only gas-liquid can fully contact, and higher mass-transfer efficiency is arranged, and the heat of solution in the mass transport process can also be removed rapidly, and the tower temperature is effectively controlled, and has quickened NH
3Fast Absorption, air film control is reasonable, and mass-transfer efficiency obviously improves, and has alleviated the load of hypomere vertical sieve tray tower tray section simultaneously, makes weak aqua ammonia propose the dense further reinforcement that is able to, and has reached the effect of limit mass transfer limit heat exchange.This also just the present invention be different from the key point that tower is cleaned in the recovery of positive element tower company.
2. the present invention is used for the comprehensive ammonia recovery of the carbonization cleaning tower of chemical fertilizer production, the synthetic recovery tower of exitting of speeding, and the cooling balancing segment tower tray number of plies is few, and (the cooling balancing segment tower tray number of plies is loaded according to production and tower outlet NH to be generally 3～6 layers
3Gas, CO
2The gas index is determined).The tower tray that heat-exchanger rig is not set adopts the vertical sieve tray tower plate structure.The vertical sieve tray tower tray belongs to the ejection-type column plate, and very high mass-transfer efficiency is arranged.Therefore, the mass-transfer efficiency of whole tower is very high.Again since the present invention according to the influence of the mass transfer load variations of whole tower and mass transfer heat of solution to mass transport process, to cool off balancing segment tower tray layer and non-cooling balancing segment tower tray layer is arranged alternately, and make its tower tray number of plies of not establishing heat-exchanger rig up and down of cooling balancing segment tower tray that is positioned at tower top greater than the tower tray number of plies of not establishing heat-exchanger rig that is positioned at the tower bottom, eliminated the mass transfer heat of solution effectively to the mass transport process adverse effect, further improve the mass-transfer efficiency of whole tower, reduced the NH during tower is worked off one's feeling vent one's spleen
3Gas, CO
2Gas content has improved the concentration of ammoniacal liquor, and ammonia has obtained recycling.
3. the present invention concentrates the gas cap that rises that tower tray replaces the prior art traditional structure with rising gas, not only than prior art to rise gas gas distribution section gas distribution more even, and increased one deck mass transfer section, be that gas had carried out one time mass transport process before entering original mass transfer absorber portion, reduced the gas transfer load.And absorption liquid has carried out absorption process one time after having finished original absorption process, has improved the concentration of absorption liquid, and absorption liquid has obtained concentrating.And the concentrated tower tray of gas that rises of the present invention belongs to bubble cap tray, and operating flexibility is big, operates steadily, and in service at tower, the gas load of tower bottom is big, and the basecoat tray design of tower is become bubble cap tray, helps improving the operating flexibility and the running stability of whole tower.
4. the Despumation device newly established of the present invention can effectively remove the liquid foam that gas is carried secretly, and this had both reclaimed effective ingredient, had also created advantage for the following road technical process of gas.
5. heat-exchanger rig of the present invention adopts bend pipe drawer-type structure heat-exchanger rig, and a plurality of separate heat-exchanger rigs (number that heat-exchanger rig is provided with is determined according to the diameter of tower) are set on the column plate, and the column plate of each layer tower tray all adopts sieve plate.Therefore, the present invention has that pressure drop is low, and anti-blockage capability is strong, and the life-span is long, and is easy for installation, and maintenance load is low.
The present invention is owing to taked multiple effective creative technical measures, technical performance is very good, compared with the prior art, mass-transfer efficiency improves about 25%, gas processing capability improves about 50%, and pressure drop is low, anti-blockage capability is strong, operating flexibility is big, operate steadily, the life-span is long, maintenance load is low.The comprehensive ammonia of carbonization that the present invention is used for fertilizer industry reclaims the cleaning tower, and the synthetic recovery tower of exitting of speeding can produce following good effect:
1. under normal operative condition, can only reclaim 2～4 tons of ammonia (calculating by producing 2.5 ten thousand tons of abilities of synthetic ammonia per year) every day in summer, weak aqua ammonia can all reclaim, and is guaranteeing under the isorrheic condition recovery tower gas vent NH more
3≤ 0.05g/m
3, CO
2≤ 0.15%, ammonia concn reaches 100～130TT, through synthetic " two gas " ammonia-cleaning tower, gas vent NH
3≤ 0.1g/m
3, and can make the ammonia concn of recovery bring up to 180～200TT.
2. the desirable fixedly recovery tower hypomere that disappears of carbonization workshop section.After transforming former comprehensive tower, can accomplish three tower Joint Production, reduce the investment of equipment, improve the production capacity of equipment.
3. " two gas " of synthesis system reclaims, and only needs that former clean ammonia is cleaned tower and transforms, and can satisfy the recovery ability of ammonia system.
4. behind employing the present invention, can improve organic efficiency, heat exchange efficiency and the output of ammonia, reduce cost, increase economic benefit and environmental protection aspect and obtain remarkable result, and can regain investment for trnasforming urban land then at water-saving and electricity-saving.
The present invention is suitable for trourelle especially and handles atm number.
The present invention reclaims cleaning tower, the synthetic recovery tower of exitting of speeding except the comprehensive ammonia of carbonization that can be widely used in the fertilizer industry, synthetic two gas recovery towers, can be applicable to well that also other industry has the mass transport process of the exothermic reaction or the endothermic reaction, can both obtain good effect.
Accompanying drawing 1 is an overall structure schematic diagram of the present invention.
Accompanying drawing 2 is structural representations of the vertical sieve tray in the accompanying drawing 1.
Below in conjunction with description of drawings, provide one embodiment of the present of invention, and by embodiment the present invention is done and to describe in further detail.
Embodiment is the industrial experiment of the present invention at Sichuan Zhong Jiang ammonia fertilizer plant.With the present invention original φ 1600/ φ 2000 of this factory being reclaimed cleaning transforms.This factory's production capacity is for producing 2.5 ten thousand tons of synthetic ammonia per year.With the natural gas is raw material, and gasification system adopts the CCR flow process, and carbonization system adopts three-column process flow.Before the transformation, reclaim to clean tower and adopt traditional bubble-cap tower, its mass-transfer efficiency is low, keeps in repair very difficultly, and equipment easily stops up.Carbonization tail gas runs height often.Adopt increasing soft water amount to control in the production, the soft water addition is per hour up to 20m
3More than, tower outlet tail gas ammonia content reaches 1.5g/m
3, weak aqua ammonia enters trench, and both contaminated environment caused the waste of ammonia and soft water again.
The scheme of transforming is the comprehensive ammonia of carbonization that former tower upper diameter is φ 1600 to be reclaimed the cleaning tower transform, the particular content of transforming is: the former tower body of φ 1600 is increased, 15 layers of tower tray are set in the tower body 1 altogether, wherein cool off 4 layers of balancing segment tower trays, 4 layers of the tower trays of cooling device promptly are set on sieve plate, 10 layers of the vertical sieve tray tower trays of cooling device are not set, and the basecoat of tower is for rising the concentrated tower tray 3 of gas, and 1.5 meters place is provided with Despumation device 9 above last layer tower tray.Cooling balancing segment tower tray layer 5 and the layout of non-cooling balancing segment tower tray layer 4 in tower, the bottom from the top of tower to tower is followed successively by: three layers of vertical sieve tray tower tray → one decks cooling balancing segment tower tray → three layers of vertical sieve tray tower tray → one decks cooling balancing segment tower tray → two layers of vertical sieve tray tower tray → one decks cooling balancing segment tower tray → one deck vertical sieve tray tower tray → one decks cooling balancing segment tower tray → one deck vertical sieve tray tower tray → one deck rise the concentrated tower tray of gas.Cooling balancing segment tower tray 5 is made of sieve plate column plate and the cooling device 6 that is placed in the bend pipe drawer-type structure on the column plate, and the heat exchanger tube axis of cooling device is parallel with tower plate surface, and the heat exchanger tube of cooling device is not higher than downflow weir.Three separate cooling devices 6 are set on one deck column plate.Non-cooling balancing segment tower tray layer is the vertical sieve tray tower tray, is made of sieve plate column plate 19 and the bubble-cap 17 that is arranged on sieve aperture 20 tops, is processed with passage 18 on the bubble-cap wall equably, and the direction of passage is vertical with the direction of sieve aperture.Bubble-cap bead face is parallel with tower plate surface and certain distance arranged.Rise gas and concentrate tower tray 3 by column plate 15,10 that are installed with on column plate rise inflator 13, constitute with calotte 12 that rises the inflator phase configuration and the ammoniacal liquor discharge connection 2 that is positioned on the column plate, calotte be installed with rise inflator above, be processed with bar shaped passage 14 around the calotte wall.Soft water entrance sleeve 8 is positioned on the last layer tower tray, weak aqua ammonia entrance sleeve 7 is positioned on the 6th layer of tower tray of counting from bottom to top, gas enters tower bottom from entrance sleeve 16, through with weak aqua ammonia, soft water mass transfer after discharge from the discharge connection 10 that is positioned at the tower body top.The 11st, the maintenance hand-hole.The all parts of tower all carry out preservative treatment four times with the epoxy resin brushing.
The comprehensive ammonia of carbonization after undergoing technological transformation with the present invention reclaims and cleans tower, (is 175m at full capacity by the trial run of driving at full capacity
3/ min), it is as follows to record the key technical indexes:
Compressor operating load: 175m
3/ min;
Soft water flow: 3.0m
3/ h;
Tower temperature: 36 ℃
Tail gas outlet NH
3Content: 0.071g/m
3
Tail gas outlet CO
2Content: 0.02%
Weak aqua ammonia concentration reaches: 74～76TT
Above test data shows that the technic index after this scrap build is better than ministry standard, has reduced internal circulating load, has saved energy consumption, has stopped the weak aqua ammonia discharging, and carbonization has realized water balance, has eliminated because of the pollution of weak aqua ammonia discharging to environment.
According to above-mentioned technic index measuring and calculating, annual 400 tons of the ammonia that reclaim are worth 720,000 yuan more; Economize on electricity 7.92KWh is worth 3.6 ten thousand yuan; Economize on water 14.4 ten thousand tons, be worth 8.64 ten thousand yuan.Economic benefit is very remarkable.
Claims (10)
1. the plate column that is used for mass-transfer process with thermal reaction, include tower body (1), tower tray, gas inlet and outlet, liquid entrance, it is characterized in that on the column plate of one deck tower tray, being provided at least the heat-exchanger rig (6) of cooling (or heating) absorption liquid, and tower tray (5) column plate that heat-exchanger rig is set is the sieve plate column plate.
2. plate column according to claim 1, the tower tray (4) that it is characterized in that not being provided with heat-exchanger rig is the vertical sieve tray tower tray.
3. plate column according to claim 1 is characterized in that the basecoat tower tray of tower concentrates tower tray (3) for the calotte formula rises gas.
4. plate column according to claim 1, the place that it is characterized in that being no less than 0.5 meter above the last layer tower tray of tower is provided with Despumation device (9).
5. plate column according to claim 2, it is characterized in that said vertical sieve tray tower tray is made of sieve plate column plate (19) and the bubble-cap (17) that is arranged on sieve aperture (20) top, be processed with the passage (18) vertical with sieve aperture (20) on the bubble-cap wall, the bead face of bubble-cap is parallel with the sieve plate face and certain interval arranged.
6. plate column according to claim 3, it is characterized in that said calotte formula rises gas and concentrates tower tray by column plate (15), be installed with and on column plate, rise inflator (13), taking over (2) with calotte that rises the inflator phase configuration (12) and fluid constitutes, calotte is arranged on and rises on the inflator, is processed with bar shaped passage (14) on the calotte wall.
7. according to claim 1 or 2 or 3 or 4 or 5 or 6 described plate columns, it is characterized in that being provided with the tower tray of heat-exchanger rig, its neighbouring tower tray is not for being provided with the tower tray of heat-exchanger rig.
8. plate column according to claim 7, it is characterized in that being no less than when two-layer when the tower tray layer that heat-exchanger rig is set, be positioned at tower top be provided with heat-exchanger rig tower tray its tower tray number of plies of heat-exchanger rig is not set up and down, greater than be positioned at the tower bottom be provided with heat-exchanger rig tower tray its tower tray number of plies of heat-exchanger rig is not set up and down.
9. plate column according to claim 8 is characterized in that said heat-exchanger rig is the heat exchanger tube axis horizontal heat exchanger parallel with the sieve plate face, and the height of heat exchanger tube is not more than the height of tower tray downflow weir.
10. plate column according to claim 9 is characterized in that said horizontal heat-exchanger rig is the bend pipe drawer-type structure, and two separate bend pipe drawer type heat-exchanger rigs are set on the tower tray at least.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97107740A CN1067598C (en) | 1997-10-27 | 1997-10-27 | Plate tower for mass-transfer process with thermal reaction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97107740A CN1067598C (en) | 1997-10-27 | 1997-10-27 | Plate tower for mass-transfer process with thermal reaction |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1215620A true CN1215620A (en) | 1999-05-05 |
| CN1067598C CN1067598C (en) | 2001-06-27 |
Family
ID=5169830
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97107740A Expired - Fee Related CN1067598C (en) | 1997-10-27 | 1997-10-27 | Plate tower for mass-transfer process with thermal reaction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1067598C (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100393392C (en) * | 2006-08-26 | 2008-06-11 | 浙江江山化工股份有限公司 | Ammonia synthesis purge gas isobaric recovery tower |
| CN102704699A (en) * | 2012-05-24 | 2012-10-03 | 大连福佳·大化石油化工有限公司 | PX (P Xylene) device absorbing tower maintenance technology |
| CN104338341A (en) * | 2014-09-30 | 2015-02-11 | 营口桃仙制药设备有限公司 | Jet type supergravity bed |
| CN106379915A (en) * | 2016-08-30 | 2017-02-08 | 贵州兴化化工股份有限公司 | Urea desorption hydrolysis tower |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1016318B (en) * | 1988-11-09 | 1992-04-22 | 余远明 | Inner unit of direct heat-exchange synthetic tower |
| CN2134219Y (en) * | 1992-09-08 | 1993-05-26 | 刘金成 | Gas-liquid contactor |
-
1997
- 1997-10-27 CN CN97107740A patent/CN1067598C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100393392C (en) * | 2006-08-26 | 2008-06-11 | 浙江江山化工股份有限公司 | Ammonia synthesis purge gas isobaric recovery tower |
| CN102704699A (en) * | 2012-05-24 | 2012-10-03 | 大连福佳·大化石油化工有限公司 | PX (P Xylene) device absorbing tower maintenance technology |
| CN102704699B (en) * | 2012-05-24 | 2014-10-15 | 大连福佳·大化石油化工有限公司 | PX (P Xylene) device absorbing tower maintenance technology |
| CN104338341A (en) * | 2014-09-30 | 2015-02-11 | 营口桃仙制药设备有限公司 | Jet type supergravity bed |
| CN104338341B (en) * | 2014-09-30 | 2015-12-30 | 辽宁桃仙制药机械设备有限公司 | A kind of injecting type hypergravity bed |
| CN106379915A (en) * | 2016-08-30 | 2017-02-08 | 贵州兴化化工股份有限公司 | Urea desorption hydrolysis tower |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1067598C (en) | 2001-06-27 |
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