CN203845829U - Ammonia absorption device for ammonia tank purge gas - Google Patents
Ammonia absorption device for ammonia tank purge gas Download PDFInfo
- Publication number
- CN203845829U CN203845829U CN201420142177.0U CN201420142177U CN203845829U CN 203845829 U CN203845829 U CN 203845829U CN 201420142177 U CN201420142177 U CN 201420142177U CN 203845829 U CN203845829 U CN 203845829U
- Authority
- CN
- China
- Prior art keywords
- ammonia
- tank
- absorption
- tower
- evaporating cold
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 209
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 102
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 53
- 238000010926 purge Methods 0.000 title abstract 4
- 238000001704 evaporation Methods 0.000 claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 8
- 238000005507 spraying Methods 0.000 claims abstract description 5
- 238000004140 cleaning Methods 0.000 claims description 43
- 238000013022 venting Methods 0.000 claims description 26
- 230000008676 import Effects 0.000 claims description 20
- 239000007921 spray Substances 0.000 claims description 12
- 238000003860 storage Methods 0.000 claims description 12
- 239000013589 supplement Substances 0.000 claims description 5
- 238000011084 recovery Methods 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 abstract 2
- 230000001502 supplementing effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 17
- 239000008234 soft water Substances 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- PPBAJDRXASKAGH-UHFFFAOYSA-N azane;urea Chemical compound N.NC(N)=O PPBAJDRXASKAGH-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 238000010010 raising Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000003643 water by type Substances 0.000 description 2
- CVOFKRWYWCSDMA-UHFFFAOYSA-N 2-chloro-n-(2,6-diethylphenyl)-n-(methoxymethyl)acetamide;2,6-dinitro-n,n-dipropyl-4-(trifluoromethyl)aniline Chemical compound CCC1=CC=CC(CC)=C1N(COC)C(=O)CCl.CCCN(CCC)C1=C([N+]([O-])=O)C=C(C(F)(F)F)C=C1[N+]([O-])=O CVOFKRWYWCSDMA-UHFFFAOYSA-N 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
Abstract
The utility model belongs to an ammonia absorption device for ammonia tank purge gas. The device comprises an ammonia purifying tower, wherein the ammonia tank purge gas is connected with an ammonia tank purge gas inlet below the ammonia purifying tower, an ammonia water outlet at the bottom of the ammonia purifying tower is connected with an ammonia water tank, a coil is arranged at the lower section of the ammonia purifying tower, a multi-layer absorption tower plate structure is arranged at the upper section of the ammonia purifying tower, an offgas outlet is arranged at the upper part of the ammonia purifying tower, a desalted water inlet is arranged at one side of the upper part of the multi-layer absorption tower plate structure, a coil outlet is connected with an evaporating cold coil inlet arranged on an evaporating cold through a compressor, a water collecting box is arranged at the bottom of the evaporating cold, a spraying water pump communicated at the lower part of the water collecting box is connected with a sprayer at the upper part inside the evaporating cold, an evaporating cold coil is arranged at the position corresponding to the lower part of the sprayer, the outlet of the evaporating cold coil is connected with the coil inlet arranged on the ammonia purifying tower sequentially through a liquid ammonia storing tank and a liquid ammonia pump, and a liquid ammonia supplementing pipeline is arranged at the top of the liquid ammonia storing tank. The ammonia absorption device has the advantages of simple structure, no waste of desalted water and high ammonia recovery efficiency.
Description
Technical field
The utility model belongs to clean ammonia absorption techniques field, is specifically related to a kind of ammonia tank ammonia absorption unit of speeding to exit.
Background technology
When Coal Chemical Industry industry synthetic ammonia or chemical fertilizers production, store the ammonia tank of liquefied ammonia because need maintain certain pressure, and put ammonia pipeline and cross the insoluble of gas and gas, need to discharge noncondensable gas, above-mentioned non-condensable gas is called the venting of speeding of ammonia tank.Speed to contain hydrogen, nitrogen, ammonia and methane in venting, flow is 2800～3300Nm
3/ h, wherein ammonia content is 15～20%, if do not recycle the loss that will cause ammonia, reduces the economic benefit of enterprise.
The ammonia-cleaning tower of at present common ammonia recovery unit, is generally all divided into upper and lower two sections, and epimere is clean ammonia device, and inner general employing bubble-cap, vertical sieve tray or float valve are mass transfer component; Hypomere is bubble level, comprises that many group water tanks carry out cooling and absorb the venting of speeding.Its shortcoming is that ammonia-cleaning tower hypomere diameter is bigger than normal, and gas-to-liquid contact is bad, need remaining ammonia in the venting of speeding be removed with a large amount of, excessive de-salted waters, has not only wasted great lot of water resources, more produces a large amount of unserviceable waste dilute ammonias.
Utility model content
The purpose of this utility model be to overcome deficiency of the prior art and provide a kind of simple in structure, do not waste de-salted water, ammonia organic efficiency is high, the ammonia tank that purified gas can do that fuel is used and strong aqua can directly the enter urea ammonia liquor storage tank ammonia absorption unit of speeding to exit.
The purpose of this utility model is achieved in that and comprises ammonia-cleaning tower, the venting of speeding of ammonia tank is connected with the ammonia tank that the is located at ammonia-cleaning tower bottom import of speeding to exit, the ammoniacal liquor outlet that is located at ammonia-cleaning tower bottom is connected with ammonia vessel, the hypomere of ammonia-cleaning tower is provided with coil pipe, the epimere of ammonia-cleaning tower is provided with the absorption tower plate structure of multilayer, the top of ammonia-cleaning tower is provided with tail gas outlet, one side on the absorption tower plate structure of multilayer top is provided with de-salted water import, coil pipe outlet is connected with the evaporating cold coil pipe import being arranged on evaporating cold by compressor, the bottom of evaporating cold is provided with header tank, the feeding spraying pump that header tank bottom is connected is connected with the spray that is arranged on evaporating cold internal upper part by spray water pipeline, spray corresponding position, bottom is provided with evaporating cold coil pipe, the outlet of evaporating cold coil pipe is connected with the coil pipe import being arranged on ammonia-cleaning tower with ammonia pump by liquefied ammonia storage tank successively, the top of described liquefied ammonia storage tank is provided with and supplements liquefied ammonia pipeline.The corresponding position of described de-salted water import internal upper part is provided with downtake.The absorption tower plate structure of described multilayer comprises that the absorption column plate of some layers is staggered, one end of the absorption column plate of some layers is fixedly installed on the inwall of ammonia-cleaning tower, the other end top of the absorption column plate of some layers is fixedly installed overflow weir, its underpart is provided with chord downcomer, and the absorption column plate of described some layers is provided with several apertures.The diameter of described aperture is 3～8mm.
The ammonia tank of making according to the such scheme ammonia absorption unit of speeding to exit, by being set, coil pipe can be good at reducing the temperature of venting of speeding, the coil pipe gas velocity of venting that can effectively delay to speed simultaneously, increase time and the area of gas-to-liquid contact, when the discharge temperature that makes to speed reduces, ammonia organic efficiency improves greatly; Simultaneously by the absorption tower plate structure of multilayer is set, that speeds that the hypomere of venting by ammonia-cleaning tower do not absorbed contact the ammonia in further absorption gas through the aperture on absorption column plate with the de-salted water from top from bottom to top containing ammonia gas, make ammonia content drop to 200PPm and go out below tower, thereby reach the object that improves ammonia recovery, make the rate of recovery of ammonia reach 99～99.8%; The qualified purified gas of tail gas outlet is sent to blowing air and can be used as fuel use, and the strong aqua in ammonia vessel can directly be sent in urea ammonia liquor storage tank and use; Have simple in structurely, do not waste de-salted water and the high advantage of ammonia organic efficiency.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model;
Fig. 2 is the structural representation of the absorption column plate of the utility model.
Embodiment
As Fig. 1, shown in 2, the utility model comprises ammonia-cleaning tower 1, the venting of speeding of ammonia tank is connected with the ammonia tank that the is located at ammonia-cleaning tower 1 bottom import 14 of speeding to exit, the ammoniacal liquor outlet 15 that is located at ammonia-cleaning tower 1 bottom is connected with ammonia vessel 16, the hypomere of ammonia-cleaning tower 1 is provided with coil pipe 3, the epimere of ammonia-cleaning tower 1 is provided with the absorption tower plate structure of multilayer, the top of ammonia-cleaning tower 1 is provided with tail gas outlet 20, one side on the absorption tower plate structure of multilayer top is provided with de-salted water import 19, coil pipe outlet 18 is connected with the evaporating cold coil pipe import 7 being arranged on evaporating cold 4 by compressor 25, the bottom of evaporating cold 4 is provided with header tank 10, the feeding spraying pump 11 that header tank 10 bottoms are connected is connected with the spray 5 that is arranged on evaporating cold 4 internal upper parts by spray water pipeline 9, spray corresponding position, 5 bottoms and be provided with evaporating cold coil pipe 6, evaporating cold coil pipe outlet 8 is connected with the coil pipe import 17 being arranged on ammonia-cleaning tower 1 with ammonia pump 12 by liquefied ammonia storage tank 13 successively, the top of described liquefied ammonia storage tank 13 is provided with and supplements liquefied ammonia pipeline 26.The corresponding position of described de-salted water import 19 internal upper parts is provided with downtake 2.The absorption tower plate structure of described multilayer comprises that the absorption column plate 21 of some layers is staggered, one end of the absorption column plate 21 of some layers is fixedly installed on the inwall of ammonia-cleaning tower 1, the other end top of the absorption column plate 21 of some layers is fixedly installed overflow weir 22, its underpart is provided with chord downcomer 23, and the absorption column plate 21 of described some layers is provided with several apertures 24.The diameter of described aperture 24 is 3～8mm.In the absorption tower plate structure of multilayer that described de-salted water enters ammonia-cleaning tower 1 epimere by de-salted water import 19, top at absorption column plate 21, inwall and overflow weir 22 by ammonia-cleaning tower 1 make de-salted water form certain height, unnecessary de-salted water flows out with chord downcomer 23 from a side of overflow weir 22 subsequently, the aperture 24 that ammonia tank speeds to exit by absorption column plate 21 upwards flows, thereby the venting that makes to speed fully contacts with de-salted water.Described liquefied ammonia storage tank 13 carries out liquefied ammonia by supplementary liquefied ammonia pipeline 26 and supplements when the utility model brings into operation, and does not need to supplement liquefied ammonia in the situation that of the normal operation of the utility model.
Principle of work of the present utility model comprises the following steps: one, pressure is 2.4～2.6MPa, temperature is 38～45 ℃, flow is that the venting of speeding of 2800～3300Nm3/h enters ammonia-cleaning tower 1 hypomere from the import 14 of speeding to exit of the ammonia tank of ammonia-cleaning tower 1 bottom, described in the volume fraction of ammonia content in venting of speeding be 15～20%; Two, the venting of speeding of 1 hypomere of the ammonia-cleaning tower described in step 1 is carried out to heat exchange with the liquefied ammonia being located in ammonia-cleaning tower 1 hypomere coil pipe 3, the discharge temperature of speeding after heat exchange is 26～30 ℃, coil pipe 3 internal pressures are 1～1.5MPa, temperature is to be evaporated to pressure 0.1～0.15MPa after the liquefied ammonia heat exchange of 32～35 ℃, and temperature is the gas ammonia of 0～5 ℃; Three, by pressure 0.1～0.15MPa after the heat exchange described in step 2, temperature is that the gas ammonia of 0～5 ℃ flows out from coil pipe outlet 18, evaporating cold coil pipe import 7 after compressor 25 pressure-raisings on evaporating cold 4 enters into evaporating cold coil pipe 6, gas ammonia pressure after described pressure-raising is 1～1.5MPa, and temperature is 70～75 ℃; Four, the soft water temperature being located in evaporating cold 4 bottom header tanks 10 is 25～28 ℃, and feeding spraying pump 11 is driven in spray 5 after the soft water in header tank 10 is pressurized to 0.4～0.5MPa; Five, the soft water in the spray described in step 45 is sprayed on evaporating cold coil pipe 6, carry out heat exchange with the high temperature gas ammonia in evaporating cold coil pipe 6, the gas ammonia cooling liquefaction that makes in evaporating cold coil pipe 6 70～75 ℃ is the liquefied ammonia of 32～35 ℃; Six, make in the coil pipe of evaporating cold described in step 56 liquefied ammonia of 32～35 ℃ enter in liquefied ammonia storage tank 13 through evaporating cold coil pipe outlet 8, then through ammonia pump 12, the liquefied ammonia in liquefied ammonia storage tank 13 is entered in coil pipe 3 by coil pipe import 17, recycle; Seven, spray described in step 5 enters in the header tank 10 of evaporating cold 4 bottoms from top to bottom to the soft water of evaporating cold coil pipe 6, completes a refrigeration cycle; Eight, flow is 1～1.8t/h, temperature is 25～30 ℃, pressure is that the de-salted water import 19 at de-salted water process ammonia-cleaning tower 1 top of 0.3～0.5MPa enters in ammonia-cleaning tower 1, through the absorption tower plate structure of multilayer, and with heat exchange described in step 2 after temperature be that counter current contact absorption is carried out in the venting of speeding of 26～30 ℃, the speeding venting after counter current contact absorbs enters some layers absorption column plate 21 place of ammonia-cleaning tower 1 epimere; The described counter current contact volume fraction of ammonia content in venting of speeding after absorbing is reduced to 2～5% by 15～20%; Nine, make to enter in step 8 ammonia-cleaning tower 1 epimere speed venting by some layers absorption column plate 21 place open aperture 24 respectively with the absorption column plate 21 of some layers in de-salted water again carry out counter current contact absorption, the venting of speeding after counter current contact absorption is discharged by the tail gas outlet 20 on ammonia-cleaning tower 1 top again, and in the speeding venting after the described absorption of counter current contact again, ammonia content is 150～200PPm; Ten, in step 9, the de-salted water containing ammonia of counter current contact after absorbing enters coil pipe 3 places of ammonia-cleaning tower 1 hypomere again, and is that counter current contact absorption is carried out in the venting of speeding of 26～30 ℃ with again entering temperature after ammonia-cleaning tower 1 hypomere heat exchange; After counter current contact absorbs, again enter the venting of speeding of ammonia-cleaning tower 1 epimere, described in the volume fraction of ammonia content in venting of speeding be 2～5%; 11, counter current contact described in step 10 absorbs the venting of speeding again enter ammonia-cleaning tower 1 epimere and carries out counter current contact absorption with the de-salted waters that again enter in the absorption column plate 21 of some layers respectively by aperture 24; 12, the de-salted water containing ammonia of counter current contact described in step 10 after absorbing counter current contact in the de-salted water containing ammonia of speeding after venting again enter ammonia-cleaning tower 1 lower end and step 8 and absorbing enters into ammonia vessel 16 storages through ammoniacal liquor outlet 15; Described is 18.0～19.0% containing ammonia de-salted water containing the massfraction of ammonia.Described step 9, step 10, step 11 and step 12 can non-stop run absorb the ammonia of speeding in venting.
Claims (4)
1. the ammonia tank ammonia absorption unit of speeding to exit, comprise ammonia-cleaning tower (1), it is characterized in that: the venting of speeding of ammonia tank is connected with the ammonia tank that is located at ammonia-cleaning tower (1) the bottom import (14) of speeding to exit, the ammoniacal liquor outlet (15) that is located at ammonia-cleaning tower (1) bottom is connected with ammonia vessel (16), the hypomere of ammonia-cleaning tower (1) is provided with coil pipe (3), the epimere of ammonia-cleaning tower (1) is provided with the absorption tower plate structure of multilayer, the top of ammonia-cleaning tower (1) is provided with tail gas outlet (20), one side on the absorption tower plate structure of multilayer top is provided with de-salted water import (19), coil pipe outlet (18) is connected with the evaporating cold coil pipe import (7) being arranged on evaporating cold (4) by compressor (25), the bottom of evaporating cold (4) is provided with header tank (10), the feeding spraying pump (11) that header tank (10) bottom is connected is connected with the spray (5) that is arranged on evaporating cold (4) internal upper part by spray water pipeline (9), spray corresponding position, (5) bottom is provided with evaporating cold coil pipe (6), evaporating cold coil pipe outlet (8) is connected with the coil pipe import (17) being arranged on ammonia-cleaning tower (1) with ammonia pump (12) by liquefied ammonia storage tank (13) successively, the top of described liquefied ammonia storage tank (13) is provided with and supplements liquefied ammonia pipeline (26).
2. the ammonia tank according to claim 1 ammonia absorption unit of speeding to exit, is characterized in that: the corresponding position of described de-salted water import (19) internal upper part is provided with downtake (2).
3. the ammonia tank according to claim 1 ammonia absorption unit of speeding to exit, it is characterized in that: the absorption tower plate structure of described multilayer comprises that the absorption column plate of some layers (21) is staggered, one end of the absorption column plate of some layers (21) is fixedly installed on the inwall of ammonia-cleaning tower (1), the other end top of the absorption column plate of some layers (21) is fixedly installed overflow weir (22), its underpart is provided with chord downcomer (23), and the absorption column plate of described some layers (21) is provided with several apertures (24).
4. the ammonia tank according to claim 3 ammonia absorption unit of speeding to exit, is characterized in that: the diameter of described aperture (24) is 3～8mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420142177.0U CN203845829U (en) | 2014-03-24 | 2014-03-24 | Ammonia absorption device for ammonia tank purge gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420142177.0U CN203845829U (en) | 2014-03-24 | 2014-03-24 | Ammonia absorption device for ammonia tank purge gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203845829U true CN203845829U (en) | 2014-09-24 |
Family
ID=51558869
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420142177.0U Expired - Lifetime CN203845829U (en) | 2014-03-24 | 2014-03-24 | Ammonia absorption device for ammonia tank purge gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203845829U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103864098A (en) * | 2014-03-24 | 2014-06-18 | 河南心连心化肥有限公司 | Ammonia absorption device for ammonia pot purge gas and absorption technology |
| CN106517243A (en) * | 2016-10-27 | 2017-03-22 | 湖南懋天世纪新材料有限公司 | High temperature ammonia recovery device |
| CN109821432A (en) * | 2019-03-20 | 2019-05-31 | 山东恒昌聚材化工科技股份有限公司 | The device of ammonium hydroxide is prepared with liquefied ammonia |
-
2014
- 2014-03-24 CN CN201420142177.0U patent/CN203845829U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103864098A (en) * | 2014-03-24 | 2014-06-18 | 河南心连心化肥有限公司 | Ammonia absorption device for ammonia pot purge gas and absorption technology |
| CN106517243A (en) * | 2016-10-27 | 2017-03-22 | 湖南懋天世纪新材料有限公司 | High temperature ammonia recovery device |
| CN106517243B (en) * | 2016-10-27 | 2018-09-18 | 湖南懋天世纪新材料有限公司 | A kind of high temperature ammonia recycling device |
| CN109821432A (en) * | 2019-03-20 | 2019-05-31 | 山东恒昌聚材化工科技股份有限公司 | The device of ammonium hydroxide is prepared with liquefied ammonia |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 453731 Xinxiang Economic Development Zone, Henan Province (Xiaoji Town) Patentee after: Henan Xinlianxin Chemical Industry Group Co.,Ltd. Address before: 453731 Henan Xinxiang Economic Development Zone Xiaoji Town Henan Xinlianxin Chemical Fertilizer Co., Ltd. Patentee before: HENAN XINLIANXIN FERTILIZER Co.,Ltd. |
|
| CP03 | Change of name, title or address | ||
| CX01 | Expiry of patent term |
Granted publication date: 20140924 |
|
| CX01 | Expiry of patent term |