CN102796571A - System for producing light benzene by performing negative pressure debenzolization on rich oil - Google Patents
System for producing light benzene by performing negative pressure debenzolization on rich oil Download PDFInfo
- Publication number
- CN102796571A CN102796571A CN2012102591435A CN201210259143A CN102796571A CN 102796571 A CN102796571 A CN 102796571A CN 2012102591435 A CN2012102591435 A CN 2012102591435A CN 201210259143 A CN201210259143 A CN 201210259143A CN 102796571 A CN102796571 A CN 102796571A
- Authority
- CN
- China
- Prior art keywords
- light benzene
- benzene
- light
- tank body
- negative pressure
- 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.)
- Granted
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a system for producing light benzene by performing negative pressure debenzolization on rich oil. The system comprises a debenzolization tower, wherein the top of the debenzolization tower is communicated with a light benzene condensation cooler through a light benzene steam pipeline, the light benzene condensation cooler is communicated with a light benzene return tank through a cooling liquid introducing pipe and a pressure balancing pipe, the light benzene return tank is connected with a light benzene return groove through a light benzene discharge pipe, the light benzene return groove is connected with the debenzolization tower through a light benzene return pipe, the light benzene return tank is provided with a non-condensable gas discharge pipe, the non-condensable gas discharge pipe is communicated with a tubular heat exchanger, a negative pressure pipe is arranged on the tubular heat exchanger, and the negative pressure pipe is communicated with a vacuum pump. The system disclosed by the invention can change ordinary pressure operation to negative pressure operation in a rich oil debenzolization distillation process, be conducive to reducing the distillation boiling point of the light benzene at the top of the tower, reduce the load of the light benzene condensation cooler, realize a smaller amount of separated water from the light benzene, eliminate the need of adopting multiple devices to separate the separated water from the light benzene, be conductive to lowering the cost of the devices, avoid great consumption of steam resources and be conductive to reducing environmental pollution.
Description
Technical field
The present invention relates to Coal Chemical Industry rich oil crude benzol Distallation systm, specifically a kind of light benzene extraction system of rich oil negative pressure benzene removal.
Background technology
At present, the whole cold wash benzene of domestic coke-oven plant gas purification workshop section all adopts tar washing oil or oil washing oil to wash the benzene in the coal gas, and washing oil absorbs benzene and becomes rich oil, becomes washing oil again or claims oil-poor after benzene is taken off in the rich oil distillation.In order to guarantee the recycle of washing oil, must remove the benzene in the rich oil, make it to become and can be sent to whole cold wash benzene workshop section and wash the oil-poor of benzene once more.In the existing all kinds of process method, the method that all adopts steamed to blow removes the crude benzol in the rich oil, and is under condition of normal pressure, to carry out.In the production process, owing to adopt steam as the distillatory thermal source, therefore, can produce a large amount of reluctant crude benzol and divide dried uply, the branch that needs a plurality of equipment of design to separate in crude benzol and the crude benzol is dried up, and the equipment self cost is higher.Expended a large amount of steam resources simultaneously, also caused serious environmental to pollute easily, the recycling economy index of advocating with country also differs greatly.
Summary of the invention
The purpose of this invention is to provide a kind of light benzene extraction system of rich oil negative pressure benzene removal, it can change the rich oil de-benzene distil process into negative-pressure operation by normal pressure, and negative pressure helps reducing the boiling point that distillates of cat head light benzene; Alleviated the load of light benzene condensate cooler, energy-saving and cost-reducing, vacuum distillation need not adopt steam as the distillatory thermal source; It is less that light benzene separates the water yield; Moisture in the rich oil, thus need not adopt the branch in a plurality of device separates light benzenes dried up, help reducing the cost of equipment self; Avoid the mass consumption of steam resource simultaneously, also help the pollution that alleviates environment.
The present invention realizes through following technical scheme for realizing above-mentioned purpose: comprise debenzolizing tower, the debenzolizing tower top is communicated with the light benzene condensate cooler through the light benzene steam pipeline; Be communicated with through quench liquid access tube and pressure equalizing pipe between light benzene condensate cooler and the light benzene return tank, light benzene return tank bottom is provided with the separated flow outlet, and the light benzene return tank is connected with the light benzene backflash through the light benzene vent pipe; The light benzene backflash is connected with debenzolizing tower through the light benzene return line, on the light benzene return line reflux pump is installed, and light benzene return tank top is provided with the noncondensable gas vent pipe; The noncondensable gas vent pipe is communicated with shell and tube heat exchanger; The shell and tube heat exchanger bottom is communicated with the light benzene return tank through collector tube, and liquid collecting pump and automatically controlled stopping valve are installed on the collector tube, and the negative pressure pipe is set on the shell and tube heat exchanger; The negative pressure pipe is communicated with vacuum pump; Liquid collecting pump, automatically controlled stopping valve and vacuum pump are connected with unit through lead respectively, and unit can cut out automatically controlled stopping valve and liquid collecting pump automatically when vacuum pump is worked, and when vacuum pump quits work, open automatically controlled stopping valve and liquid collecting pump automatically; The light benzene return tank comprises horizontal tank body; Horizontal tank base mid-way is communicated with the top of vertical tank body, and horizontal tank base is connected with the light benzene vent pipe, and vertical tank base is provided with the separated flow outlet; Horizontal inner tank wall is provided with the annular brace muscle, and through hole is offered in annular brace muscle bottom.The quench liquid access tube extends in horizontal tank body near horizontal tank base, and quench liquid access tube and light benzene vent pipe are separately positioned on vertical tank body both sides, and overflow plate is installed in the horizontal tank body between light benzene vent pipe and the vertical tank body.Quench liquid access tube lower end is provided with hydraucone.On the horizontal inner tank wall at light benzene vent pipe place vortex shield is set.
The invention has the advantages that: it can change the rich oil de-benzene distil process into negative-pressure operation by normal pressure; Vacuum distillation need not adopt steam as the distillatory thermal source; It is less that light benzene separates the water yield; Moisture in the rich oil, thus need not adopt the branch in a plurality of device separates light benzenes dried up, reduced the cost of equipment self; Avoid the mass consumption of steam resource, also helped the pollution that alleviates environment; Light benzene extraction efficient is high, and can reduce debenzolizing tower cat head light benzene steam extraction temperature, helps reducing the load of condensation refrigerating unit, improves condensation efficiency, and then reaches the effect that improves the light benzene organic efficiency etc.
Description of drawings
Fig. 1 is a structural representation of the present invention; Fig. 2 is the structural representation of light benzene return tank according to the invention.
Embodiment
The light benzene extraction system of a kind of rich oil negative pressure benzene removal of the present invention comprises debenzolizing tower 1, and debenzolizing tower 1 top is communicated with light benzene condensate cooler 3 through light benzene steam pipeline 2; Is communicated with through quench liquid access tube 5 and pressure equalizing pipe 6 between light benzene condensate cooler 3 and the light benzene return tank 4, light benzene return tank 4 bottoms are provided with separated flow outlet 7, and light benzene return tank 4 passes through light benzene vent pipe 8 and is connected with light benzene backflash 9; Light benzene backflash 9 is connected with debenzolizing tower 1 through light benzene return line 10, and reflux pump 11 is installed on the light benzene return line 10, and light benzene return tank 4 tops are provided with noncondensable gas vent pipe 12; Noncondensable gas vent pipe 12 is communicated with shell and tube heat exchanger 13; Shell and tube heat exchanger 13 bottoms are communicated with light benzene return tank 4 through collector tube 14, and liquid collecting pump 24 and automatically controlled stopping valve 26 are installed on the collector tube 14, and negative pressure pipe 15 is set on the shell and tube heat exchanger 13; Negative pressure pipe 15 is communicated with vacuum pump 16; Liquid collecting pump 24, automatically controlled stopping valve 26 and vacuum pump 16 are connected with unit 25 through lead respectively, and unit 25 can cut out automatically controlled stopping valve 26 and liquid collecting pump 24 automatically when vacuum pump 16 work, when vacuum pump 16 quits work, open automatically controlled stopping valve 26 and liquid collecting pump 24 automatically; Light benzene return tank 4 comprises horizontal tank body 17; Mid-way, horizontal tank body 17 bottom is communicated with the top of vertical tank body 18, and horizontal tank body 17 bottoms are connected with light benzene vent pipe 8, and vertical tank body 18 bottoms are provided with separated flow outlet 7; Horizontal tank body 17 inwalls are provided with annular brace muscle 21, and through hole 23 is offered in annular brace muscle 21 bottoms.Debenzolizing tower 1, light benzene condensate cooler 3, light benzene return tank 4 and shell and tube heat exchanger 13 all keep negative pressure state under the effect of vacuum pump 16; Pressure in vacuum pump 16 and the shell and tube heat exchanger 13 are about-60 KPa to-70KPa; Pressure in light benzene condensate cooler 3 and the light benzene return tank 4 is about-55 KPa to-65 KPa; When the pressure of debenzolizing tower 1 cat head was about-50 to-60 KPa aforesaid devices and is in this pressure range, the light benzene extraction was most effective, and can tower top temperature be controlled at 70 ℃ to 80 ℃; And present tower top temperature of the prior art is all between 90 ℃ to 95 ℃; Tower top temperature reduces the load that can effectively reduce the condensation refrigerating unit, improves condensation efficiency, and then reaches the effect that improves the light benzene organic efficiency.Owing to constantly have quench liquid to pass through in the quench liquid access tube 5; Therefore must between light benzene condensate cooler 3 and light benzene return tank 4, pressure equalizing pipe 6 be set; Otherwise light benzene condensate cooler 3 can't keep identical constantly with pressure between the light benzene return tank 4; If difference appears in the pressure between light benzene condensate cooler 3 and the light benzene return tank 4; Can cause raising gradually, cause to keep the ideal negative pressure in the debenzolizing tower 1, influence the light benzene formation efficiency from light benzene condensate cooler 3 to debenzolizing tower 1 each device interior pressure.The light benzene steam that debenzolizing tower 1 cat head is discharged gets into light benzene condensate cooler 3 through light benzene steam pipeline 2; Condensed quench liquid gets into light benzene return tank 4 through quench liquid access tube 5 in the light benzene condensate cooler 3; After light benzene and the water sepn, divide and dried uply discharge from separating water out 7, light benzene gets into light benzene backflashes 9 through light benzene vent pipe 8; A part of light benzene is back to debenzolizing tower 1 through light benzene return line 10 in the light benzene backflash 9 under the effect of reflux pump 11, and remaining light benzene is as the product extraction; Gas suction shell and tube heat exchanger 13 under suction function in the light benzene return tank 4; Light benzene steam residual in the gas can condensation become phlegma in shell and tube heat exchanger 13; Get back to once more in the light benzene return tank 4 and separate; Remaining noncondensable gas gets into the negative pressure gas line through vacuum pump 16, is convenient to collection and treatment.Because shell and tube heat exchanger 13 inside be negative pressure, therefore need installation liquid collecting pump 24 on collector tube 14, through the liquid collecting pump 24 phlegma blowback light benzene return tank 4 that shell and tube heat exchanger 13 is interior; When preventing vacuum pump 16 work with the gas in the light benzene return tank 4 from collector tube 14 suction shell and tube heat exchanger 13; Cause heat exchange efficiency to reduce, influence condensation effect, need on collector tube 14, to install automatically controlled stopping valve 26; When vacuum pump 16 work; With collector tube 14 sealings, prevent that gas from from collector tube 14 suction shell and tube heat exchanger 13, helping improving the light benzene organic efficiency through automatically controlled stopping valve 26.Because light benzene return tank 4 tank bodies need bear bigger negative pressure pressure; As adopt existing light benzene return tank 4 tank bodies the situation of indent distortion can occur; The present invention is for addressing this problem; Horizontal tank body 17 inwalls at light benzene return tank 4 are provided with annular brace muscle 21, for guaranteeing the both sides liquid conducting of annular brace muscle, offer through hole 23 in annular brace muscle 21 bottoms.The present invention can change the rich oil de-benzene distil process into negative-pressure operation by normal pressure, has alleviated the load of light benzene condensate cooler, and is energy-saving and cost-reducing; Vacuum distillation need not adopt steam as the distillatory thermal source, and it is less that light benzene separates the water yield, moisture in the rich oil; Thereby need not adopt the branch in a plurality of device separates light benzenes dried up; Reduce the cost of equipment self, avoided the mass consumption of steam resource simultaneously, also helped the pollution that alleviates environment.
The present invention is in order to strengthen the light benzene separating effect of light benzene withdrawing can 4; Can adopt following structure: quench liquid access tube 5 extends in horizontal tank body 17 near horizontal tank body 17 bottoms; Quench liquid access tube 5 is separately positioned on vertical tank body 18 both sides with light benzene vent pipe 8, in the horizontal tank body 17 between light benzene vent pipe 8 and the vertical tank body 18 overflow plate 20 is installed.Flow velocity when 5 outlets of quench liquid access tube can reduce quench liquid entering light benzene return tank 4 near horizontal tank body 17 bottoms; Reduce the disturbance of quench liquid to liquid in the light benzene return tank 4; Overflow plate 20 is separated into two portions with horizontal tank body 17, when liquid level rises to overflow plate 20 tops, just flow to a side that is provided with light benzene vent pipe 8; When quench liquid got into horizontal tank body 17, the liquid of light benzene vent pipe 8 one sides received disturbance hardly.
Flow velocity when the present invention gets into light benzene return tank 4 in order further to reduce quench liquid, the light benzene separating effect of enhancing light benzene withdrawing can 4 can be provided with hydraucone 19 in quench liquid access tube 5 lower ends.When liquid was flowed through hydraucone 19 from pipeline, because diameter increases, flow velocity can reduce automatically.
The present invention forms eddy current when preventing the discharge opeing of light benzene vent pipe 8 places, causes the light benzene outflow resistance to increase, and can on horizontal tank body 17 inwalls at light benzene vent pipe 8 places, vortex shield 22 be set.
Claims (4)
1. the light benzene extraction system of a rich oil negative pressure benzene removal; Comprise debenzolizing tower (1); Debenzolizing tower (1) top is communicated with light benzene condensate cooler (3) through light benzene steam pipeline (2); It is characterized in that: be communicated with through quench liquid access tube (5) and pressure equalizing pipe (6) between light benzene condensate cooler (3) and the light benzene return tank (4); Light benzene return tank (4) bottom is provided with separated flow outlet (7), and light benzene return tank (4) is connected with light benzene backflash (9) through light benzene vent pipe (8), and light benzene backflash (9) is connected with debenzolizing tower (1) through light benzene return line (10); Light benzene return line (10) is gone up reflux pump (11) is installed; Light benzene return tank (4) top is provided with noncondensable gas vent pipe (12), and noncondensable gas vent pipe (12) is communicated with shell and tube heat exchanger (13), and shell and tube heat exchanger (13) bottom is communicated with light benzene return tank (4) through collector tube (14); Collector tube (14) is gone up liquid collecting pump (24) and automatically controlled stopping valve (26) is installed; Negative pressure pipe (15) is set on the shell and tube heat exchanger (13), and negative pressure pipe (15) is communicated with vacuum pump (16), and liquid collecting pump (24), automatically controlled stopping valve (26) and vacuum pump (16) are connected with unit (25) through lead respectively; Unit (25) can cut out automatically controlled stopping valve (26) and liquid collecting pump (24) automatically when vacuum pump (16) is worked; Automatically open automatically controlled stopping valve (26) and liquid collecting pump (24) when quitting work when vacuum pump (16), light benzene return tank (4) comprises horizontal tank body (17), and mid-way, horizontal tank body (17) bottom is communicated with the top of vertical tank body (18); Horizontal tank body (17) bottom is connected with light benzene vent pipe (8); Vertical tank body (18) bottom is provided with separated flow outlet (7), and horizontal tank body (17) inwall is provided with annular brace muscle (21), and through hole (23) is offered in annular brace muscle (21) bottom.
2. the light benzene extraction system of a kind of rich oil negative pressure benzene removal according to claim 1; It is characterized in that: quench liquid access tube (5) extends in horizontal tank body (17) near horizontal tank body (17) bottom; Quench liquid access tube (5) is separately positioned on vertical tank body (18) both sides with light benzene vent pipe (8), and overflow plate (20) is installed in the horizontal tank body (17) between light benzene vent pipe (8) and the vertical tank body (18).
3. the light benzene extraction system of a kind of rich oil negative pressure benzene removal according to claim 1 and 2 is characterized in that: quench liquid access tube (5) lower end is provided with hydraucone (19).
4. the light benzene extraction system of a kind of rich oil negative pressure benzene removal according to claim 1 and 2 is characterized in that: on horizontal tank body (17) inwall that light benzene vent pipe (8) is located vortex shield (22) is set.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210259143.5A CN102796571B (en) | 2012-07-25 | 2012-07-25 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210259143.5A CN102796571B (en) | 2012-07-25 | 2012-07-25 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102796571A true CN102796571A (en) | 2012-11-28 |
| CN102796571B CN102796571B (en) | 2014-04-30 |
Family
ID=47195882
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210259143.5A Active CN102796571B (en) | 2012-07-25 | 2012-07-25 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102796571B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103160334A (en) * | 2013-03-14 | 2013-06-19 | 济钢集团有限公司 | Method and device for separation of benzene and water in debenzolized rich oil |
| CN105062575A (en) * | 2015-08-03 | 2015-11-18 | 中冶焦耐工程技术有限公司 | Process and apparatus for controlling continuous and stable discharge of non-condensable gas in benzene recovery system |
| CN106139626A (en) * | 2016-08-25 | 2016-11-23 | 山东恒导石油化工股份有限公司 | The online air stripping of organic heat carrier removes technique and the device cracking light component |
| CN110484289A (en) * | 2019-09-24 | 2019-11-22 | 济宁黑猫炭黑有限责任公司 | A kind of tar negative pressure dewatering system and method |
| CN115487520A (en) * | 2022-08-31 | 2022-12-20 | 扬州中惠制药有限公司 | Time-sharing and fixed-delivery extraction equipment for various traditional Chinese medicines |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100530330B1 (en) * | 2001-11-27 | 2005-11-22 | 주식회사 포스코 | Method for oil separation from cokes oven gas |
| CN101544913A (en) * | 2009-05-04 | 2009-09-30 | 济南冶金化工设备有限公司 | Process and equipment for negative pressure benzene removal |
| CN201543262U (en) * | 2009-11-27 | 2010-08-11 | 盂县中信焦化有限公司 | Crude benzene condenser for coking use |
| CN201603409U (en) * | 2009-12-26 | 2010-10-13 | 太原化工股份有限公司 | Crude benzol reduced pressure distillation device |
| CN102199070A (en) * | 2011-04-06 | 2011-09-28 | 上海同特化工科技有限公司 | Tubular furnace method pressure-reduced debenzolization and distillation process |
| CN102408298A (en) * | 2011-09-21 | 2012-04-11 | 宝钢工程技术集团有限公司 | Method of distilling crude benzene by decompression method and device thereof |
-
2012
- 2012-07-25 CN CN201210259143.5A patent/CN102796571B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100530330B1 (en) * | 2001-11-27 | 2005-11-22 | 주식회사 포스코 | Method for oil separation from cokes oven gas |
| CN101544913A (en) * | 2009-05-04 | 2009-09-30 | 济南冶金化工设备有限公司 | Process and equipment for negative pressure benzene removal |
| CN201543262U (en) * | 2009-11-27 | 2010-08-11 | 盂县中信焦化有限公司 | Crude benzene condenser for coking use |
| CN201603409U (en) * | 2009-12-26 | 2010-10-13 | 太原化工股份有限公司 | Crude benzol reduced pressure distillation device |
| CN102199070A (en) * | 2011-04-06 | 2011-09-28 | 上海同特化工科技有限公司 | Tubular furnace method pressure-reduced debenzolization and distillation process |
| CN102408298A (en) * | 2011-09-21 | 2012-04-11 | 宝钢工程技术集团有限公司 | Method of distilling crude benzene by decompression method and device thereof |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103160334A (en) * | 2013-03-14 | 2013-06-19 | 济钢集团有限公司 | Method and device for separation of benzene and water in debenzolized rich oil |
| CN105062575A (en) * | 2015-08-03 | 2015-11-18 | 中冶焦耐工程技术有限公司 | Process and apparatus for controlling continuous and stable discharge of non-condensable gas in benzene recovery system |
| CN106139626A (en) * | 2016-08-25 | 2016-11-23 | 山东恒导石油化工股份有限公司 | The online air stripping of organic heat carrier removes technique and the device cracking light component |
| CN106139626B (en) * | 2016-08-25 | 2018-05-08 | 山东恒利热载体工程技术有限公司 | The online air lift of organic heat carrier removes the technique and device of cracking light component |
| CN110484289A (en) * | 2019-09-24 | 2019-11-22 | 济宁黑猫炭黑有限责任公司 | A kind of tar negative pressure dewatering system and method |
| CN115487520A (en) * | 2022-08-31 | 2022-12-20 | 扬州中惠制药有限公司 | Time-sharing and fixed-delivery extraction equipment for various traditional Chinese medicines |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102796571B (en) | 2014-04-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101544913B (en) | Process and equipment for negative pressure benzene removal | |
| CN102796571B (en) | System for producing light benzene by performing negative pressure debenzolization on rich oil | |
| CN106477792A (en) | A kind of method and device for stripping process petrochemical industry sour water nothing side line single column negative pressure | |
| CN101475435A (en) | Method for preparing industrial naphthalin by single-furnace double-tower vacuum distillation | |
| CN204932917U (en) | Extractive distillation device in a kind of hydrofining process of crude benzene | |
| CN106746118A (en) | A kind of system and method for utilization heat recovery from sewage alcohol ketone | |
| CN203916121U (en) | DMAC reclaims physical property index optimization system | |
| CN203886221U (en) | Light benzol and heavy benzol separation device | |
| CN112280599B (en) | Vertical multistage heating and distillation integrated wash oil regeneration equipment | |
| CN203916122U (en) | A kind of dimethylbenzene separator | |
| CN204079900U (en) | A kind of ramp type anti-coking oil header | |
| CN205042179U (en) | A condensation knockout tower for oiliness steam is handled | |
| CN203227321U (en) | Stabilization tower | |
| CN202376786U (en) | Oil-enriched negative-pressure debenzoilized light benzene condensing and cooling backflow equipment | |
| CN206152398U (en) | Solvent can palingenetic phosphoric acid by wet process extraction system | |
| CN202376785U (en) | Oil-rich negative-pressure debenzolization return tank | |
| CN217323987U (en) | Two-tower type debenzolization system | |
| CN201534001U (en) | Washing oil regenerating column | |
| CN205223134U (en) | Short-flow recovery system for separating light tar by air-float tar device | |
| CN104277858B (en) | A kind of oil shale distillation shale oil and gas phase separating technology | |
| CN217578742U (en) | Solvent recovery refining plant in synthetic rubber production process | |
| CN216738224U (en) | Solvent refining system in process of preparing base oil from waste lubricating oil | |
| CN203886220U (en) | Pre-distillation device | |
| CN221084690U (en) | Device for coupling coking crude benzene distillation with ammonia distillation waste heat | |
| CN203904293U (en) | Detarring and moisture removing purifying device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |