CN204251370U - Alcohol natural pond liquid deamination equipment - Google Patents
Alcohol natural pond liquid deamination equipment Download PDFInfo
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- CN204251370U CN204251370U CN201420717307.9U CN201420717307U CN204251370U CN 204251370 U CN204251370 U CN 204251370U CN 201420717307 U CN201420717307 U CN 201420717307U CN 204251370 U CN204251370 U CN 204251370U
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- deammoniation
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Abstract
This device belongs to deammoniation nitrogen technical field, First Heat Exchanger, the second interchanger, deammoniation tower, scrubber tower and compressor is comprised in particular to a kind of alcohol natural pond liquid deamination equipment, First Heat Exchanger is connected with the second interchanger, second interchanger connects deammoniation tower, deammoniation tower side connects raw steam and enters pipe, top connects scrubber tower, bottom connects kettle-type reboiler entrance and discharging pump respectively, discharging pump connects the second interchanger, scrubber tower top connects compressor inlet, and compressor outlet connects kettle-type reboiler.In this device deammoniation tower tower, ascending vapor is mainly water vapor, and the ammonia that more general hot blast has stronger ability to deviate from material divides; Compressor makes the gas phase after except ammonia heat up, and makes it possess and reheat the ability that material generates new round gas phase in kettle-type reboiler, allow the generation of new round gas phase not at the energy depending on raw steam.Vacuum pump then extracts non-condensable gases out system, ensure that the lower concentration of carbonic acid gas in system, and what ensure that ammonia divides continues efficiently to deviate from.
Description
Technical field
The utility model relates to a kind of alcohol natural pond liquid deamination equipment, belongs to deammoniation nitrogen technical field.
Background technology
Deammoniation nitrogen treatment process in the industry for alcohol natural pond liquid class material is in a bottleneck stage always.Usual employing be blow-off method, and ammonia still process method.Blow-off method needs more than 55 degree a large amount of gases to carry out stripping to the ammonia in water body, is roughly 1500 ~ 2000 side's gas and could processes one ton of water.The use and its hot gas cannot reflux for a long time, because deamination is along with the process of decarbonation, carbonic acid gas accumulation in system can cause the stripping of ammonia in water body suppressed.And often need more than the PH pre-treatment to 10 by material, to reach good deamination effect.Then cannot deamination efficiently for the low PH material of the weakly alkaline that PH8 is such.Therefore, under the state that the treatment process of current this kind of material is also in a high energy consumption, the market requirement of this utility model is defined.
Utility model content
The technical problems to be solved in the utility model is: provide a kind of minimizing gas phase usage quantity, improve ammonia removal efficiency and can reduce processing cost, realize gas phase recycle, the alcohol natural pond liquid deamination equipment of increasing work efficiency.
Alcohol natural pond described in the utility model liquid deamination equipment comprises First Heat Exchanger, the second interchanger, deammoniation tower, scrubber tower and compressor, First Heat Exchanger is connected with the second interchanger, second interchanger connects deammoniation tower, deammoniation tower side connects raw steam and enters pipe, top connects scrubber tower, and bottom connects kettle-type reboiler entrance and discharging pump respectively, and discharging pump connects the second interchanger, scrubber tower top connects compressor inlet, and compressor outlet connects kettle-type reboiler.
Alcohol natural pond liquid first enters First Heat Exchanger and water of condensation carries out heat exchange, and material obtains preliminary preheating, and water of condensation is cooled, and is conducive to vacuum tightness and realizes.Material enters the second interchanger again, heats the material after preheating, and heat interchanging area is enough large, to make between low 3 ~ 10 degree of bubble point temperature in material ratio tower.Material after heat exchange fully enters deammoniation tower and utilizes raw steam to carry out deamination, raw steam enters pipe by raw steam and enters in deammoniation tower tower body, after deamination, material is exported by discharging pump at the bottom of deammoniation tower tower, enters the second interchanger, with the starting material heat exchange entering the second interchanger.Gas phase with ammonia exports from deammoniation tower tower top, enters scrubber tower.In scrubber tower, dilute sulphuric acid carries out gas washing to gas phase, removes ammonia in gas phase and divides.Steam after deamination exports from scrubber tower tower top again, and the compressor that leads, gas phase is compressed intensification 5 to 20 DEG C by compressor, and the kettle-type reboiler that leads, gas phase self condensation, the secondary steam produced that boils again carries out heating deamination to material together with raw steam, and in deammoniation tower, produce new round gas phase, and this circulation continues always.
Described compressor outlet connects raw steam and enters pipe, and compressor drive shaft place arranges raw steam and enters pipe, arranges return line between compressor outlet and compressor inlet.Lead to acting as of the steam of driven compressor direction of principal axis and sealing is provided.Seal form is steam seal.The raw steam leading to compressor outlet steam-pipe is the water vapor in order to make compressor also can provide sufficient temp when self providing enough temperature rises, to ensure the operation of compressor continued smooth.From compressor outlet backflow to the water vapor of compressor inlet be in order to balance compressor import and export between unnecessary pressure reduction, to ensure that compressor runs stably.
Described kettle-type reboiler outlet connects First Heat Exchanger by water pump, and First Heat Exchanger connects solidifying water pot, and solidifying water pot top connects vacuum pump, and bottom arranges outlet, and connects compressor by water pump.The solidifying water produced in kettle-type reboiler carries out preliminary preheating to First Heat Exchanger to material by water pump.Solidifying water flows into solidifying water pot from First Heat Exchanger again.Small portion coagulate solidifying water in water pot under the effect of water pump pump to compressor, as the overheated elimination water of compressor.The solidifying water of major part pumps whole unit by water pump.
Scrubber tower is not only represent its ammonia can sloughed in gas phase to divide, and it can be divided into multiple absorption tower to reclaim and remove in gas phase useful profitable or can cause dysgenic component to compressor operating in concrete technology flow process.This is the means that the present invention reduces costs further, is also the core technology ensureing the smooth running of system energy when being applied to concrete case.Invent corresponding natural pond liquid for this, if deviate from hypercapnia in the liquid of natural pond, then need to carry out gas washing to it with sodium hydroxide gas washing tower before gas phase enters compressor, absorb carbonic acid gas wherein.Otherwise will greatly increase the cost of compressor operating load and compressor.Vacuum tightness determines service temperature during deamination of the present invention.The force value detected in kettle-type reboiler is elected at its reference mark as.Reason is that the duct length of distance vacuum pump is here maximum, and tower bottom pressure is greater than tower top.When vacuum tightness is up to standard herein, system vacuum is up to standard.Gas washing effect is that the amount measuring ascending vapor (water vapor) ensures.But feeding preheating effect is difficult to reach bubble point, so the heat of the raw steam of needs makes material reach bubble point.Otherwise fall in process the water vapor condensation that can make in the gas phase of rising on material, cause gas phase to reduce, new circulation does not reach the requirement of design deamination.So need to pass into appropriate water vapor.But when selecting reference mark and control method, at the bottom of simple detection tower, in tower, the temperature of tower top to ensure that the flow of gas phase is enough.So the present invention selects the gas flow surveying deammoniation tower tower top suitable to ensure the degree of deamination in deammoniation tower tower.But be not only containing water vapor in gas phase, the carbonic acid gas deviate from and ammonia also can occupy volumetric flow rate, so the material needs of different components could determine the operation controling parameters of its correspondence after testing.More can the scrubber tower of lifting system economy can be installed additional.The operating mode of these scrubber towers is identical with scrubber tower.
Compared with the automatic control of compressor manages with traditional industries, the present invention has only made and has a bit changed.The temperature out of compressor, no longer has relation with temperature in deammoniation tower tower, but is directly set in a temperature, up to standardly sends.Its meaning is that the raw steam that compressor outlet passes into can not be used further to charging to be warming up to bubble point.Its main reason is the air output that in the case used of the present invention, inlet amount is far longer than compressor, by steam this pass into can unnecessary walk a segment pipe, increase calorific loss, not as in direct feeding deammoniation tower.Secondary cause is, a large amount of raw steam is led and overheat of compressor may be caused to eliminate the abnormal work of pump into compressor outlet, because a large amount of raw steam sharply can raise the temperature of compressor outlet, causes overheated elimination pump warning spray cooling.In addition compressor inlet outlet pressure differential variable valve is also a ring standing in robot control system(RCS).
The beneficial effects of the utility model are:
In deammoniation tower tower, ascending vapor is mainly water vapor, and the ammonia that more general hot blast has stronger ability to deviate from material divides; Compressor makes the gas phase after except ammonia heat up, and makes it possess and reheat the ability that material generates new round gas phase in kettle-type reboiler, allow the generation of new round gas phase not at the energy depending on raw steam.Vacuum pump then extracts non-condensable gases (being mainly carbonic acid gas) out system, ensure that the lower concentration of carbonic acid gas in system, and what ensure that ammonia divides continues efficiently to deviate from.First Heat Exchanger and the second interchanger have then fully retained heat energy valuable in system as two interchanger that system is imported and exported, and make charging not need to give birth to steam in a large number to heat up and can reach bubble point, this is the basis of hi-temp hi-effective ammonia still process.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
In figure: 1, the second interchanger 2, First Heat Exchanger 3, vacuum pump 4, solidifying water pot 5, raw steam enter pipe 6, deammoniation tower 7, kettle-type reboiler 8, discharging pump 9, scrubber tower 10, compressor inlet 11, compressor outlet 12, compressor 13, raw vapour source 14, material discharge nozzle 15, material enter pipe 16, return line.
Embodiment
Below in conjunction with accompanying drawing, the utility model is described further:
As shown in Figure 1, alcohol natural pond described in the utility model liquid deamination technique equipment comprises First Heat Exchanger 2, second interchanger 1, deammoniation tower 6, scrubber tower 9 and compressor 12, First Heat Exchanger 2 is connected with the second interchanger 1, second interchanger 1 connects deammoniation tower 6, deammoniation tower 6 side connects raw steam and enters pipe 5, raw steam enters pipe 5 and connects raw vapour source 13, deammoniation tower 6 top connects scrubber tower 9 by pipeline, bottom connects entrance and the discharging pump 8 of kettle-type reboiler 7 respectively, discharging pump 8 connects the second interchanger 1 by pipeline, scrubber tower 9 top connects compressor inlet 10, compressor outlet 11 connects kettle-type reboiler 7.Compressor outlet 11 connects raw vapour source 13 or raw steam enters pipe 5, and compressor drive shaft place arranges raw steam and enters pipe 5, arranges return line 16 between compressor outlet 11 and compressor inlet 10.Kettle-type reboiler 7 exports and connects First Heat Exchanger 2 by water pump, and First Heat Exchanger 2 connects solidifying water pot 4, and solidifying water pot 4 top connects vacuum pump 3, and bottom arranges outlet, and connects compressor 12 by water pump.
Alcohol natural pond liquid deamination process is:
(1) to the preliminary preheating of alcohol natural pond liquid: alcohol natural pond liquid enters pipe 15 by material and passes in First Heat Exchanger 2, the water of condensation produced in kettle-type reboiler 7 can be utilized the preliminary preheating of alcohol natural pond liquid, temperature after preliminary preheating rises 0.5 ~ 5 DEG C, the water of condensation produced in kettle-type reboiler 7 is passed in First Heat Exchanger 2 with the liquid heat exchange of alcohol natural pond;
(2) to the alcohol natural pond liquid heating after preliminary preheating, make bubble point temperature 3 ~ 10 degree in charging final distance tower 6, the material that deammoniation tower 6 tower bottom flow can be utilized to go out is to the alcohol natural pond liquid heating after preheating, the material that deammoniation tower 6 tower bottom flow goes out is passed in the second interchanger 1, carry out heat exchange with the alcohol natural pond liquid after preliminary preheating, final material flows out from material discharge nozzle 14;
(3) secondary steam utilizing raw steam and reboiler to produce is to the alcohol natural pond liquid deamination after heating, after deamination, material exports the second interchanger 1 to, gas phase with ammonia passes into by dilute sulphuric acid gas washing in scrubber tower 9, and remove ammonia in gas phase and divide, the temperature of raw steam is 100 DEG C ~ 150 DEG C;
(4) gas phase after deamination exports from scrubber tower 9 tower top, and the compressor 12 that leads, gas phase compression is elevated the temperature 5 ~ 20 degree by compressor 12, gas phase after heating up is imported kettle-type reboiler 7, new round secondary steam is produced, new round secondary steam heats deamination to alcohol natural pond liquid together with raw steam in deammoniation tower 6, and new round secondary steam forms the gas phase of a new round together with raw steam, recycles.The temperature of secondary steam is 55 DEG C ~ 100 DEG C.In compressor 12 working process, pass into raw steam to driven compressor direction of principal axis, play sealing function; Pipeline to compressor outlet 11 passes into raw steam, compressor 12 can be made when self cannot provide enough temperature rises also to provide the water vapor of sufficient temp, to ensure the operation of compressor 12 continued smooth.Compressor outlet 11, to compressor inlet 10 recirculation water steam, can balance pressure reduction unnecessary between compressor import and export, to ensure that compressor runs stably.
(5) the solidifying water produced in kettle-type reboiler 7 carries out preliminary preheating by water pump to First Heat Exchanger 2 pairs of materials.Solidifying water flows into solidifying water pot 4 from First Heat Exchanger 2 again.Small portion coagulate solidifying water in water pot 4 under the effect of water pump pump to compressor 12, as the overheated elimination water of compressor 12.The solidifying water of major part pumps whole unit by water pump.
Claims (3)
1. an alcohol natural pond liquid deamination equipment, it is characterized in that: comprise First Heat Exchanger (2), second interchanger (1), deammoniation tower (6), scrubber tower (9) and compressor (12), First Heat Exchanger (2) is connected with the second interchanger (1), second interchanger (1) connects deammoniation tower (6), deammoniation tower (6) side connects raw steam and enters pipe (5), top connects scrubber tower (9), bottom connects kettle-type reboiler (7) entrance and discharging pump (8) respectively, discharging pump (8) connects the second interchanger (1), scrubber tower (9) top connects compressor inlet (10), compressor outlet (11) connects kettle-type reboiler (7).
2. alcohol natural pond according to claim 1 liquid deamination equipment, it is characterized in that: compressor outlet (11) connects raw steam and enters pipe (5), compressor drive shaft place arranges raw steam and enters pipe (5), arranges return line (16) between compressor outlet (11) and compressor inlet (10).
3. alcohol natural pond according to claim 1 and 2 liquid deamination equipment, it is characterized in that: kettle-type reboiler (7) outlet connects First Heat Exchanger (2) by water pump, First Heat Exchanger (1) connects solidifying water pot (4), solidifying water pot (4) top connects vacuum pump (3), bottom arranges outlet, and connects compressor (12) by water pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420717307.9U CN204251370U (en) | 2014-11-25 | 2014-11-25 | Alcohol natural pond liquid deamination equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420717307.9U CN204251370U (en) | 2014-11-25 | 2014-11-25 | Alcohol natural pond liquid deamination equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204251370U true CN204251370U (en) | 2015-04-08 |
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ID=52955698
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420717307.9U Expired - Fee Related CN204251370U (en) | 2014-11-25 | 2014-11-25 | Alcohol natural pond liquid deamination equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204251370U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445476A (en) * | 2014-11-25 | 2015-03-25 | 徐翔 | Ethyl alcohol biogas slurry deamination technology and equipment |
| CN106315726A (en) * | 2016-10-12 | 2017-01-11 | 江苏金茂源生物化工有限责任公司 | Biogas slurry decarbonization and deamination combined system |
-
2014
- 2014-11-25 CN CN201420717307.9U patent/CN204251370U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445476A (en) * | 2014-11-25 | 2015-03-25 | 徐翔 | Ethyl alcohol biogas slurry deamination technology and equipment |
| CN106315726A (en) * | 2016-10-12 | 2017-01-11 | 江苏金茂源生物化工有限责任公司 | Biogas slurry decarbonization and deamination combined system |
| CN106315726B (en) * | 2016-10-12 | 2019-05-03 | 江苏金茂源生物化工有限责任公司 | A kind of biogas slurry decarburization combining deamination system |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Jiangsu Hecheng Pharmaceutical Equipment Manufacturing Co., Ltd. Assignor: Xu Xiang Contract record no.: 2015320000546 Denomination of utility model: Alcohol biogas slurry deamination equipment Granted publication date: 20150408 License type: Exclusive License Record date: 20150715 |
|
| LICC | Enforcement, change and cancellation of record of contracts on the licence for exploitation of a patent or utility model | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150408 Termination date: 20161125 |