CN208517188U - A kind of Containing-Sulfur Wastewater Treatment System - Google Patents
A kind of Containing-Sulfur Wastewater Treatment System Download PDFInfo
- Publication number
- CN208517188U CN208517188U CN201821004722.4U CN201821004722U CN208517188U CN 208517188 U CN208517188 U CN 208517188U CN 201821004722 U CN201821004722 U CN 201821004722U CN 208517188 U CN208517188 U CN 208517188U
- Authority
- CN
- China
- Prior art keywords
- water
- pipeline
- stripper
- sent
- tank
- 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 - Fee Related
Links
Landscapes
- Physical Water Treatments (AREA)
Abstract
A kind of Containing-Sulfur Wastewater Treatment System, belong to oil refining field, if including stripper, raw water flash tank, raw material water tank, booster pump, oil expeller, tower top feed pump, tower top cold feed cooler, raw water head tank, cold feed heat exchanger, level-one segregator, two-stage fractional condensation device, three-level condensate cooler, reboiler, sour gas liquid separation tank and trunk pipeline etc..The raw water that the utility model mixes the raw water of de-oiling with three-level segregator phegma replaces purified water as tower top cold feed, realize that the effect of mild washing absorption ammonia is pushed up in the control of tower top cold feed, to reduce circulation inside purified water, acidic water stripping device processing load is reduced.
Description
Technical field
The utility model relates to arrive oil refining field, specifically a kind of Containing-Sulfur Wastewater Treatment System.
Background technique
In large-scale Petrochemical Enterprises, each oil refining apparatus, including atmospheric and vacuum distillation unit, catalytic cracking unit, diesel oil hydrogenation
Device, Wax Oil Hydrogenation Unit, hydrocracking unit, coking plant, solvent deasphalting unit, sulfur recovery facility etc., normal
It can be generated in production process a certain amount of sour water (also known as acid water or raw water), sour water is due to containing a certain amount of
Ammonia nitrogen, sulfide and oil gas, handled by acidic water stripping device (also known as sewage stripping device), successively by de- hydrocarbon, de-
The purified water of qualified is obtained after oil, stripper stripping, purified water can be back to each device in upstream and (such as be used as instead of demineralized water
Electric desalting apparatus water filling etc.), extra purified water drains into sewage farm outside.Acidic water stripping device described herein uses single column
Pressurization stripping side line takes out ammonia process, i.e. stripper top generates sour gas (main component is hydrogen sulfide), the thick ammonia of lateral line withdrawal function
(main component is vapor and ammonia) generates high concentration ammonia after three-level condenses, and three-level segregator segregates liquid reflux, tower bottom
Generate purified water.
Under normal circumstances, sour water (hydrogenation type raw water) hydrogen sulfide and the ammonia-nitrogen content for being related to hydrogenation plant are higher,
Average ammonia-nitrogen content 3000-10000mg/L, average sulfide contents 3000-15000mg/L.Hydrogenation type raw water and acid water
The fractional condensation liquid mixing that stripper plant lateral line withdrawal function part three-level segregator generates, generation are averaged ammonia-nitrogen content into tower raw water
7000-20000mg/L.When acidic water stripping device handles hydrogenation type raw water, stripper feed design is divided into three parts, by upper
It is followed successively by under tower top cold feed (raw material is purified water), the cold feed of middle and upper part and hot feed are into tower raw water.
According to different practice in factory, purified water ammonia control difference refers to the purified water that acidic water stripping device generates
It marks, under normal circumstances purified water ammonia nitrogen ≯ 100mg/L, hydrogen sulfide ≯ 20mg/L.Using purified water as tower top cold feed, mainly
Control top temperature is acted through, ammonia in stripper upper gaseous phase is washed, guarantees concentration of hydrogen sulfide in sour gas.
It is such that purified water is used to have the following problems for the mode of tower top cold feed: (1) using product purified water be used as into
Material, in a disguised form increases acidic water stripping device treating capacity and load；(2) circulation inside purified water increases sewage stripping dress
The steam consumption set, increases operating cost；(3) due to containing certain ammonia nitrogen in purified water, washing absorption ammonia is influenced
Effect.
Utility model content
To solve to use purified water for the above problem existing for tower top cold feed in the prior art, the utility model is provided
A kind of Containing-Sulfur Wastewater Treatment System, the raw water that the raw water of de-oiling is mixed with three-level segregator phegma are made instead of purified water
For tower top cold feed, realizes that the effect of mild washing absorption ammonia is pushed up in the control of tower top cold feed, followed inside purified water to reduce
Ring reduces acidic water stripping device processing load.
Technical solutions adopted by the utility model to solve the above technical problems are as follows: a kind of Containing-Sulfur Wastewater Treatment System,
Including stripper, raw water flash tank, raw material water tank, level-one segregator, two-stage fractional condensation device, three-level condensate cooler and sour gas
Liquid separation tank, wherein sour water is entered in raw water flash tank by raw material water pipeline flash off lighter hydrocarbons gas after pass through pipe again
Line I is sent in raw material water tank, and then passes through one by booster pump after sedimentation oil removing or " tank in tank " oil removing in raw material water tank
Secondary de-oiling water pipeline extraction is sent to secondary oil removing in oil expeller, and secondary de-oiling water pipeline is connected in the outlet of oil expeller, and
The end of secondary de-oiling water pipeline is divided into two branches, wherein by tower top feed pump to be transported to tower top cold feed cold for a branch
But stripper top is sent to by tower top cold feed pipeline after cooling in device, another branch enters raw water by pipeline II
In head tank, and then by raw material water pump by being divided into two parts after drawing it out into tower raw material water pipeline, a part is through cold feed
Stripper top is sent to by cold feed pipeline after heat exchanger is cooling, another part successively passes through two-stage fractional condensation liquid cooler, original
By hot feed pipe after material water-purified water first-class heat exchanger, level-one condensate cooler and raw water-purified water secondary heat exchanger heat exchange
Line is sent in stripper；The bottom side of the stripper is communicated with reboiler by pipeline, and the raw water in stripper exists
Under the heating stripping effect of reboiling, the high-concentration acidic wastewater gas of generation is discharged into sour gas by the acid gas pipeline of stripper top
In liquid separation tank, the high-concentration acidic wastewater gas after the separation of sour gas liquid separation tank is transported in sulfur recovery facility by pipeline III；Institute
It states the high temperature purification water generated in stripper to be discharged by the purification water pipeline of tower bottom, and successively passes through raw water-purified water second level
Heat exchanger heat release, raw water-purified water first-class heat exchanger heat release, the cooling of purified water air cooler and the cooling heel row of purified water water cooler
Out；The ammonia-containing gas generated in the stripper pass through level-one condensation cooling by the ammonia pipeline discharge in the middle part of stripper
It is sent in level-one segregator after device heat exchange, ammonia-containing gas isolate gas phase portion and fractional condensation liquid two in level-one segregator
Point, gas phase portion by gas phase discharge pipe I be sent into B-grade condensation cooler it is cooling after be discharged into two-stage fractional condensation device again into
Row separation, the gas phase portion that two-stage fractional condensation device is isolated are sent to three-level after being sent into heat exchanger cooling by gas phase discharge pipe II
Third time separation is carried out in condensate cooler, the thick ammonia for separating generation is discharged by thick ammonia discharge pipe；The level-one fractional condensation
The fractional condensation liquid generated in device and two-stage fractional condensation device passes through fractional condensation liquid discharge pipe I respectively and fractional condensation liquid discharge pipe II is imported into the
After in two mixing fractional condensation liquid pipe lines, then fractional condensation liquid pipe line is mixed by first after two-stage fractional condensation liquid cooler is cooling and is sent to pipeline
It II or is also fed into the fractional condensation liquid in tower raw material water pipeline, generated in the three-level condensate cooler through segregating liquid discharge pipe III
It is mixed in the first mixing fractional condensation liquid pipe line.
In the utility model, sour water is first sent to after the filtering of raw material water filter through filtering by the raw material water pipeline
Water pipeline is sent in raw water flash tank.
In the utility model, the stripper bottom is provided with extraction pipeline, and the extraction pipeline is by the raw material in stripper
Water draws stripper and is sent to heating stripping in reboiler, and is re-introduced into stripper by introduction pipe line.
Compared with prior art, the utility model has the following beneficial effects:
1) raw water that the utility model mixes the raw water of de-oiling with three-level segregator phegma is made instead of purified water
For tower top cold feed, realizes that the effect of mild washing absorption ammonia is pushed up in the control of tower top cold feed, followed inside purified water to reduce
Ring reduces acidic water stripping device processing load；
2) raw water that the utility model mixes the raw water of de-oiling with three-level segregator phegma is made instead of purified water
For tower top cold feed, the raw water inlet amount of acidic water stripping device is increased, improves the processing effect of acidic water stripping device
Rate reduces steam mono-consumption, reduces device operating cost；
3) raw water that the utility model mixes the raw water of de-oiling with three-level segregator phegma is made instead of purified water
For tower top cold feed, hydrogen sulfide content is higher in tower top cold feed, can preferably carry out washing absorption ammonia, improve acidity
Makings amount；
4) raw water that the utility model mixes the raw water of de-oiling with three-level segregator phegma is made instead of purified water
For tower top cold feed, reduces in sour gas and improve sour gas quality containing ammonia, provide guarantee for sulfur recovery facility even running.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the utility model；
Appended drawing reference: 1, raw material water pipeline, 2, raw material water filter, 3, filtering water pipeline, 4, raw water flash tank, 5, pipe
Line I, 6, raw material water tank, 7, de-oiling water pipelines, 8, booster pump, 9, oil expeller, 10, secondary de-oiling water pipeline, 11, tower top into
Material pump, 12, tower top cold feed cooler, 13, tower top cold feed pipeline, 14, pipeline II, 15, raw water head tank, 16, into tower
Raw material water pipeline, the 17, first mixing fractional condensation liquid pipe line, 18, raw material water pump, 19, cold feed heat exchanger, 20, cold feed pipeline,
21, stripper, 22, two-stage fractional condensation liquid cooler, 23, raw water-purified water first-class heat exchanger, 24, level-one condensate cooler,
25, raw water-purified water secondary heat exchanger, 26, hot feed pipeline, 27, acid gas pipeline, 28, sour gas liquid separation tank, 29, pipe
Line III, 30, reboiler, 31, ammonia pipeline, 32, purification water pipeline, 33, level-one segregator, 34, gas phase discharge pipe I, 35, point
Drip pipe line I, 36, B-grade condensation cooler, 37, two-stage fractional condensation device, 38, gas phase discharge pipe II, 39, fractional condensation liquid discharge
The mixing fractional condensation liquid pipe line of pipeline II, 40, second, 41, heat exchanger, 42, three-level condensate cooler, 43, thick ammonia discharge pipe,
44, liquid discharge pipe III, 45, purified water air cooler, 46, purified water water cooler are segregated.
Specific embodiment
The technical solution of the utility model is further elaborated combined with specific embodiments below.
As shown in Figure 1, a kind of Containing-Sulfur Wastewater Treatment System, including stripper 21, raw water flash tank 4, raw material water tank 6,
Level-one segregator 33, two-stage fractional condensation device 37, three-level condensate cooler 42 and sour gas liquid separation tank 28, wherein sour water passes through
Raw material water pipeline 1 enters in raw water flash tank 4 flash off lighter hydrocarbons gas after be sent in raw material water tank 6 by pipeline I 5 again,
And then it is sent by booster pump 8 by an extraction of de-oiling water pipeline 7 after sedimentation oil removing or " tank in tank " oil removing in raw material water tank 6
Enter into oil expeller 9 secondary oil removing, secondary de-oiling water pipeline 10, and secondary de-oiling water pipeline are connected in the outlet of oil expeller 9
10 end is divided into two branches, wherein branch be transported to by tower top feed pump 11 it is cold in tower top cold feed cooler 12
But the top of stripper 21 is sent to by tower top cold feed pipeline 13 after, another branch by pipeline II 14 enter raw water into
In batch can 15, and then by raw material water pump 18 by being divided into two parts after drawing it out into tower raw material water pipeline 16, a part is through cold
21 top of stripper is sent to by cold feed pipeline 20 after feed exchanger 19 is cooling, another part successively passes through two-stage fractional condensation liquid
Cooler 22, raw water-purified water first-class heat exchanger 23, level-one condensate cooler 24 and raw water-purified water secondary heat exchanger
It is sent in stripper 21 after 25 heat exchange by hot feed pipeline 26；The bottom side of the stripper 21 is communicated with weight by pipeline
Device 30 is boiled, for the raw water in stripper 21 under the heating stripping effect of reboiler 30, the high-concentration acidic wastewater gas of generation passes through vapour
The acid gas pipeline 27 at 21 top of stripper is discharged into sour gas liquid separation tank 28, highly concentrated after the separation of sour gas liquid separation tank 28
Degree sour gas is transported in sulfur recovery facility by pipeline III 29；The high temperature purification water generated in the stripper 21 is by tower bottom
It purifies water pipeline 32 to be discharged, and is successively changed by raw water -25 heat release of purified water secondary heat exchanger, raw water-purified water level-one
It is discharged after hot 23 heat release of device, the cooling of purified water air cooler 45 and the cooling of purified water water cooler 46；It is generated in the stripper 21
Ammonia-containing gas are discharged by the ammonia pipeline 31 at 21 middle part of stripper, and are sent to one after the heat exchange of level-one condensate cooler 24
In grade segregator 33, ammonia-containing gas isolate gas phase portion and fractional condensation liquid two parts in level-one segregator 33, and gas phase portion is logical
It crosses after the feeding B-grade condensation cooler 36 of gas phase discharge pipe I 34 cools down to be discharged into two-stage fractional condensation device 37 and be separated again,
The gas phase portion that two-stage fractional condensation device 37 is isolated is sent into after heat exchanger 41 cools down by gas phase discharge pipe II 38 and is sent to three-level
Third time separation is carried out in condensate cooler 42, the thick ammonia for separating generation is discharged by thick ammonia discharge pipe 43；The level-one
The fractional condensation liquid generated in segregator 33 and two-stage fractional condensation device 37 passes through fractional condensation liquid discharge pipe I 35 and fractional condensation liquid discharge pipe respectively
After II 39 are imported into the second mixing fractional condensation liquid pipe line 40, then by the first mixing fractional condensation after two-stage fractional condensation liquid cooler 22 is cooling
Liquid pipe line 17 is sent to pipeline II 14 or into the fractional condensation liquid in tower raw material water pipeline 16, generated in the three-level condensate cooler 42
It is also fed into through fractional condensation liquid discharge pipe III 44 into the first mixing fractional condensation liquid pipe line 17 and is mixed.
In the utility model, the raw material water pipeline 1 first by sour water be sent to raw material water filter 2 filter after by
Drainage pipeline 3 is sent in raw water flash tank 4.
In the utility model, 21 bottom of stripper is provided with extraction pipeline, which will be in stripper 21
Raw water draws stripper 21 and is sent to heating stripping in reboiler 30, and is re-introduced into stripper 21 by introduction pipe line
It is interior.
Claims (3)
1. a kind of Containing-Sulfur Wastewater Treatment System, it is characterised in that: including stripper (21), raw water flash tank (4), raw material water tank
(6), level-one segregator (33), two-stage fractional condensation device (37), three-level condensate cooler (42) and sour gas liquid separation tank (28), wherein
Sour water is entered in raw water flash tank (4) by raw material water pipeline (1) flash off lighter hydrocarbons gas after again by pipeline I (5)
Be sent in raw material water tank (6), so in raw material water tank (6) after sedimentation oil removing or " tank in tank " oil removing by booster pump (8)
It is sent to secondary oil removing in oil expeller (9) by de-oiling water pipeline (7) extraction, is connected with two in the outlet of oil expeller (9)
Secondary de-oiling water pipeline (10), and the end of secondary de-oiling water pipeline (10) is divided into two branches, wherein a branch passes through tower top
Feed pump (11) is transported in tower top cold feed cooler (12) and is sent to stripper by tower top cold feed pipeline (13) after cooling
(21) top, another branch are entered in raw water head tank (15) by pipeline II (14), and then by raw material water pump (18)
By being divided into two parts after drawing it out into tower raw material water pipeline (16), a part is after cold feed heat exchanger (19) are cooling by cold
Feeding line (20) is sent at the top of stripper (21), and another part successively passes through two-stage fractional condensation liquid cooler (22), raw water-
After the heat exchange of purified water first-class heat exchanger (23), level-one condensate cooler (24) and raw water-purified water secondary heat exchanger (25) by
Hot feed pipeline (26) is sent in stripper (21)；The bottom side of the stripper (21) is communicated with reboiler by pipeline
(30), under the heating stripping effect of reboiler (30), the high-concentration acidic wastewater gas of generation passes through the raw water in stripper (21)
Acid gas pipeline (27) at the top of stripper (21) is discharged into sour gas liquid separation tank (28), by sour gas liquid separation tank (28) point
High-concentration acidic wastewater gas from after is transported in sulfur recovery facility by pipeline III (29)；The high temperature generated in the stripper (21)
Purified water is discharged by the purification water pipeline (32) of tower bottom, and successively passes through raw water-purified water secondary heat exchanger (25) heat release, original
Expect water-purified water first-class heat exchanger (23) heat release, purified water air cooler (45) cooling and purified water water cooler (46) cooling heel row
Out；The ammonia-containing gas generated in the stripper (21) are passed through by ammonia pipeline (31) discharge in the middle part of stripper (21)
It is sent in level-one segregator (33) after level-one condensate cooler (24) heat exchange, ammonia-containing gas separation in level-one segregator (33)
Gas phase portion and fractional condensation liquid two parts, gas phase portion are sent into B-grade condensation cooler (36) by gas phase discharge pipe I (34) out
It is discharged into after cooling in two-stage fractional condensation device (37) and is separated again, the gas phase portion that two-stage fractional condensation device (37) is isolated passes through gas
Phase discharge pipe II (38) is sent to progress third time separation in three-level condensate cooler (42) after being sent into heat exchanger (41) cooling,
The thick ammonia that separation generates is discharged by thick ammonia discharge pipe (43)；In the level-one segregator (33) and two-stage fractional condensation device (37)
The fractional condensation liquid of generation passes through fractional condensation liquid discharge pipe I (35) respectively and fractional condensation liquid discharge pipe II (39) is imported into the second mixing point
After in lime set pipeline (40), then liquid pipe line (17) are segregated by the first mixing after two-stage fractional condensation liquid cooler (22) is cooling and are sent to
Pipeline II (14) is interior into tower raw material water pipeline (16), and the fractional condensation liquid generated in the three-level condensate cooler (42) is through segregating liquid
Discharge pipe III (44) is also fed into the first mixing fractional condensation liquid pipe line (17) and is mixed.
2. a kind of Containing-Sulfur Wastewater Treatment System according to claim 1, it is characterised in that: the raw material water pipeline (1) is first
Sour water is sent to after raw material water filter (2) filtering and is sent in raw water flash tank (4) through filtering water pipeline (3).
3. a kind of Containing-Sulfur Wastewater Treatment System according to claim 1, it is characterised in that: stripper (21) bottom is set
It is equipped with extraction pipeline, which draws stripper (21) for the raw water in stripper (21) and be sent in reboiler (30)
Heating stripping, and be re-introduced into stripper (21) by introduction pipe line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821004722.4U CN208517188U (en) | 2018-06-28 | 2018-06-28 | A kind of Containing-Sulfur Wastewater Treatment System |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821004722.4U CN208517188U (en) | 2018-06-28 | 2018-06-28 | A kind of Containing-Sulfur Wastewater Treatment System |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208517188U true CN208517188U (en) | 2019-02-19 |
Family
ID=65337427
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821004722.4U Expired - Fee Related CN208517188U (en) | 2018-06-28 | 2018-06-28 | A kind of Containing-Sulfur Wastewater Treatment System |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208517188U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109879342A (en) * | 2019-04-23 | 2019-06-14 | 宁波马克斯迈环保科技有限公司 | Soul water stripper distillate heat utilization device and method |
| CN113896265A (en) * | 2021-11-02 | 2022-01-07 | 天津市创举科技股份有限公司 | Ammonia distillation treatment process for residual ammonia water |
| CN114906897A (en) * | 2022-06-10 | 2022-08-16 | 爱智环境科技(西安)有限公司 | Coking wastewater ammonia distillation treatment device and process method |
-
2018
- 2018-06-28 CN CN201821004722.4U patent/CN208517188U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109879342A (en) * | 2019-04-23 | 2019-06-14 | 宁波马克斯迈环保科技有限公司 | Soul water stripper distillate heat utilization device and method |
| CN109879342B (en) * | 2019-04-23 | 2024-04-26 | 宁波马克斯迈环保科技有限公司 | Sour water stripper distillate heat utilization device and method |
| CN113896265A (en) * | 2021-11-02 | 2022-01-07 | 天津市创举科技股份有限公司 | Ammonia distillation treatment process for residual ammonia water |
| CN114906897A (en) * | 2022-06-10 | 2022-08-16 | 爱智环境科技(西安)有限公司 | Coking wastewater ammonia distillation treatment device and process method |
| CN114906897B (en) * | 2022-06-10 | 2024-02-09 | 爱智环境科技(西安)有限公司 | Coking wastewater ammonia distillation treatment device and process method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN208517188U (en) | A kind of Containing-Sulfur Wastewater Treatment System | |
| CN101580457B (en) | Device and process for preparing absolute ethyl alcohol by taking fermented liquor as the raw material | |
| CN102153449B (en) | Continuous refining separation device and method for coal gasification crude phenol | |
| CN109704366B (en) | Pressurized deacidification ammonia distillation heat coupling process and system | |
| CN105967425A (en) | Coal chemical industry grey water flashing treatment system capable of reducing ammonia accumulation and coal chemical industry grey water flashing treatment process capable of reducing ammonia accumulation | |
| CN104843816B (en) | A kind of heat pump flash distillation stripping deamination coproduction of ammonia sulfate and the method for ammonia | |
| CN106477792A (en) | A kind of method and device for stripping process petrochemical industry sour water nothing side line single column negative pressure | |
| CN109369419A (en) | The process and device of triethylamine are separated in a kind of industrial wastes | |
| CN102241453A (en) | Method for treating coal gasification wastewater containing phenol and ammonia | |
| CN103073145A (en) | System for recovering light oil from residual ammonia water | |
| CN104151135A (en) | Molassess raw material top-grade alcohol distillation and waste liquid concentration thermal coupling device and process | |
| CN105198711A (en) | Coked crude phenol refining device and method | |
| CN102634381B (en) | System and method for treating benzene-contained separating water of coking benzol | |
| CN104724778A (en) | Method for salt extraction from desulfurization waste solution through multi-effect evaporation | |
| CN102311771B (en) | Crude oil processing method | |
| CN104232133A (en) | Method and device for reducing potassium and sodium ion content of coal tar | |
| CN103084004A (en) | Coke cooling water and coke cutting water mutually combined purifying and recycling method | |
| CN206027129U (en) | High yield distillation system of propane diamine production line | |
| CN213012433U (en) | Acidic water treatment system | |
| CN204111354U (en) | A kind of sour water steam stripping at reduced pressure device | |
| CN201952379U (en) | Continuous refining and separating device of gasified crude phenol | |
| RU2546677C1 (en) | Method and installation of hydrocracking with obtaining motor fuels | |
| CN209778320U (en) | System for coupling heat of pressurization deacidification ammonia distillation | |
| CN205838778U (en) | A kind of sewage stripping after-purification water pre-treatment means | |
| CN102443408B (en) | Pressure reduction distillation process method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| 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: 20190219 Termination date: 20190628 |