CN102373066B - Process for treating salt deposition in fractionating tower - Google Patents
Process for treating salt deposition in fractionating tower Download PDFInfo
- Publication number
- CN102373066B CN102373066B CN201010256526.8A CN201010256526A CN102373066B CN 102373066 B CN102373066 B CN 102373066B CN 201010256526 A CN201010256526 A CN 201010256526A CN 102373066 B CN102373066 B CN 102373066B
- Authority
- CN
- China
- Prior art keywords
- weight
- salt coagulation
- coagulation inhibitor
- salt
- tower
- 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.)
- Active
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention discloses a process for treating salt deposition in a fractionating tower. A purpose of the present invention is to overcome disadvantages of time consuming, device shutdown or amount reducing, hidden danger of corrosion, and the like in the prior art, wherein the amount is the amount of the deposited salt. The method comprises that: a salt deposition inhibitor is consecutively added to the an oil product before the oil product enters a tower top reflux pipeline of the fractionating tower or a tower top circulating pump inlet of the fractionating tower, wherein 30-60 mg of the salt deposition inhibitor is added to per kg of the oil product in the tower top reflux pipeline of the fractionating tower or the tower top circulating pump inlet of the fractionating tower, the adding time is 30-60 hours, the salt deposition inhibitor comprises, by weight, 30-70% of an aliphatic nitrogen compound, 10-30% of alkyl alcohol and 20-40% of an organic solvent.
Description
Technical field
The bright oil refining apparatus corrosion control field that belongs to of this law, more particularly relate to a kind of technique of processing the oil refining apparatus salt crust, is specially adapted to process the ammonium salt scale problems of catalytic cracking unit and delayed coking unit separation column.
Background technology
In recent years along with the development trend of crude oil heaviness, in poor quality, and market is to the significantly rising of light-end products demand, and crude oil depth is processed into the main direction of oil refining industry development.Wherein heavy oil fluid catalytic cracking and delay coking process, as the Main Means of heavy oil lighting, more and more obtain the extensive attention of oil refining industry.Contain the assorted elements such as higher N, S, O, Cl in delayed coking unit or heavy oil catalytically cracking equipment raw material, at high temperature reaction is easy to generate NH
3, H
2the products such as S, the heat absorption hydrolysis reaction occurs in butter and organic chloride, decomposes and produces HCl.The gas phase NH that follows raw material to respond and generate
3and HCl, hybrid reaction oil gas enters separation column.Rising along with oil gas in separation column, in tower, temperature also has high step-down, when temperature is down to 330 ℃ of left and right, NH
3be combined with HCl and generate NH
4cl, NH
4cl is carried to the upper strata tower tray with superfine little particle by oil gas, when temperature is down to 140 ℃ of left and right and is followed oil gas continue to rise and temperature while constantly descending, NH in oil gas
4the concentrated dehydration of Cl becomes crystal, mixes with impurity such as iron rust, coke powder powder and is deposited on tower tray, downtake, is subject to liquid bath, extracts pipeline, trim the top of column line and the pump housing etc. out and locate.Can hinder flowing of oil gas when salt crust is lighter, after the obstruction tower tray, cause the separation column pressure drop to increase gradually, destroy the normal running of separation column, affect the oil separating effect; Cause and rush tower and flooding when serious, make operation disorderly, even occluding device is to produce normally to move.While NH
4the salt crust of Cl causes serious underdeposit corrosion to equipment.
Salt crust for fractionator overhead tower tray and trim the top of column line, domestic delayed coking unit and catalytic cracking unit separation column are substantially all the methods that adopts washing to process, the principle of washing is exactly that water dissolves the solid ammonium salt, take ammonium salt out of separation column by the aqueous solution, although the details of washing is slightly different, for example some uses deaerated water, and some uses fresh water, but washing principle and flow process are roughly the same.Process the main promising shut-down washing of washing process and the online washing of salt coagulation of fractionating tower, the washing of stopping work needs to cut off charging, and this flow process is the separation column outer circulation, then by the separation column crestal waterflood, is washed, and this method is not only time-consuming but also loss is larger; Online washing need to first reduce the Raw material processing amount while processing; then strengthen separation column cold reflux and top quantity of reflux; tower top temperature is reduced; and squeeze into a certain amount of cold reflux fresh water with the tower top recycle pump in outlet; fresh water and tower top turning oil are mixed into separation column; rinse and dissolve the salt crust at the positions such as tower tray, downtake; then washing water and partial reflux distillate are extracted out through the tower top recycle pump; then entering the raw gasline tank separates; this method often can be taken light cycle oil in oily(waste)water to, and the NH dissolved in water washing process
4cl flows to lower one deck tower tray with the liquid-phase reflux in tower, with temperature, raises gradually, easily causes the salt crust position move down and can not eliminate salt crust fully.In addition the washing treating processes in, NH
4the Cl aqueous solution has stronger corrodibility to equipment and pipeline, and at flow velocity, the heavy corrosion of equipment is caused at lower position after assembling.
" contemporary chemical industry ", 2004, a kind of method of processing salt crust of washing is disclosed in 33 (4), it is for the separation column of salt crust, by reducing the method for fractionator overhead temperature, increasing steam condensate and fresh water, dissolve the salt crust on wash tray and downtake, recovery operation rapidly, alleviate financial loss.Also can prevent by the method for strengthening electric desalting operation and the design of improvement separation column the generation of salt coagulation of fractionating tower in addition.This technology is the improvement on water washing treatment method, can in not shut-down situation, process the salt coagulation of fractionating tower problem.But the method need to the amount of falling, reduce fractionation tower top temperature, and has underdeposit corrosion hidden danger.
" oil Refining Technologies and engineering ", disclose a kind of method of processing salt crust of washing in 2009,39 (3), and it is the situation for delayed coking unit separation column head tower dish salt crust, points out that online washing is comparatively effectively solution of separation column head tower dish salt crust.Can push up the measures such as returning the tower temperature that circulates and prevent the salt coagulation of fractionating tower problem by guaranteeing original desalting effect, suitable by-passing portions top turning oil, control in addition.But this technology is traditional water washing treatment method, and in treating processes, separation column stops charging, cooling washing, and complex disposal process.
Summary of the invention
The purpose of this invention is to provide a kind of technique of processing catalytic cracking unit and delayed coking unit salt coagulation of fractionating tower, to overcome prior art, exist time-consuming, device to stop work or the shortcomings such as the amount of falling and Corrosion Potential.
The invention provides a kind of technique of processing salt coagulation of fractionating tower, it is characterized in that: the trim the top of column pipeline at separation column adds a kind of salt coagulation inhibitor continuously, salt coagulation inhibitor with enter separation column after oil product in the trim the top of column pipeline mixes, 30～60mg/kg that the add-on of salt coagulation inhibitor is oil product flow in the trim the top of column pipeline, the joining day is 30～60 hours.
The invention provides the another kind of technique of processing salt coagulation of fractionating tower, it is characterized in that: before the tower top pump entry of separation column, add continuously a kind of salt coagulation inhibitor, salt coagulation inhibitor with enter separation column after the oil product at tower top pump entry place mixes, 30～60mg/kg that the add-on of salt coagulation inhibitor is tower top pump entry place oil product flow, the joining day is 30～60 hours.
The invention provides the another kind of technique of processing salt coagulation of fractionating tower, it is characterized in that: before the trim the top of column pipeline of separation column and tower top pump entry, add continuously a kind of salt coagulation inhibitor, salt coagulation inhibitor with enter separation column after the oil product at trim the top of column pipeline and tower top pump entry place mixes, 30～60mg/kg that the add-on of salt coagulation inhibitor is trim the top of column pipeline and tower top pump entry place oil product flow, the joining day is 30～60 hours.
Salt coagulation inhibitor of the present invention is comprised of following component:
(A) 30～70 % by weight fat nitrogenous compounds, preferred content is 50～65 % by weight;
(B) 10～30 % by weight alkyl alcohols, preferred content is 15～25 % by weight;
(C) 20～40 % by weight organic solvents, preferred content is 20～30 % by weight.
In the salt coagulation inhibitor gross weight.
Described fatty nitrogenous compound is C
6～C
18any one in aliphatic amide or two kinds, preferably C
8～C
12any one in aliphatic amide or two kinds.
Described alkyl alcohol is C
3～C
5any one or two kinds in alkyl monocarbon alcohol or dibasic alcohol.
Described organic solvent is C
7～C
12any one or two kinds in aromatic hydrocarbons.
Salt coagulation inhibitor of the present invention adopts the mode of former dose of injection.
Technique of the present invention can be used for preventing the ammonium salt fouling and corrosion in oil refining apparatus, mainly for the treatment of the fouling and corrosion problem of the chlorination ammonium salt in catalytic cracking unit and delayed coking unit separation column.
The present invention processes the salt coagulation of fractionating tower technology with current washing and compares, and has the following advantages: (1) the present invention has advantages of that execute-in-place is easy, safety saves time and is with low cost, avoided water washing treatment method time-consuming, the shortcoming that the amount of falling or device are stopped work.(2) the present invention by inhibitor by dirty salt NH
4cl is converted into oil soluble salt, reaches the salt crust problem of eliminating ammonium chloride in separation column, makes the rapid recovery operation of separation column of salt crust.(3) the present invention is by eliminating dirty salt NH in separation column
4cl, thus the ammonium salt underdeposit corrosion in separation column avoided.
Below by the drawings and specific embodiments, describe the present invention in detail, but do not limit the scope of the invention.
Accompanying drawing and accompanying drawing explanation
Fig. 1 is the process flow diagram that a kind of processing of the present invention has the salt coagulation of fractionating tower of the tower top recycle system.
Fig. 2 is the process flow diagram that a kind of processing of the present invention does not have the salt coagulation of fractionating tower of the tower top recycle system.
In figure:
The 1-salt coagulation inhibitor, 2-tower top recycle pump, the 3-overhead heat exchanger, 4-follows air cooler, 5-separation column, 6-oil gas, 7-distillate, 8-trim the top of column line in top.
Embodiment
Separation column shown in Fig. 1 has the tower top recycle system, as shown in Figure 1, before salt coagulation inhibitor 1 is injected into the entrance of tower top recycle pump 2 continuously, salt coagulation inhibitor 1 mixes with tower top turning oil, then after following air cooler 4, overhead heat exchanger 3 and top enter separation column 5, at the interior salt coagulation inhibitor 1 of separation column 5, with the liquid phase in tower, to the lower floor of tower, flow, the NH in flow process in tower
4the Cl settling gradually in suppressed dose solvent composition infiltrate, make NH
4cl separates from metallic surface, the NH in salt coagulation inhibitor 1 in active ingredient fat nitrogenous compound and tower
4the Cl reaction, discharge NH
3the tower top that rises to separation column 5 with oil gas 6 is discharged, and the oil soluble salt of generation is dissolved in the distillate of corresponding boiling range, then with distillate 7, takes separation column out of.
Separation column shown in Fig. 2 does not have the tower top recycle system, as shown in Figure 2, salt coagulation inhibitor 1 is injected into to trim the top of column line 8, salt coagulation inhibitor 1 with enter separation column 5 after trimming oil in trim the top of column line 8 mixes, salt coagulation inhibitor 1 flows to the lower floor of tower with the liquid phase in tower, the NH in flow process in tower
4the Cl settling gradually in suppressed dose solvent composition infiltrate, make NH
4cl separates from metallic surface, the NH in inhibitor in active ingredient fat nitrogenous compound and tower
4the Cl reaction, discharge NH
3rise to separation column 5 tower tops with oil gas 6 and discharge, the oil soluble salt of generation is dissolved in the distillate of corresponding boiling range, then with distillate 7, takes separation column out of.
Embodiment
The present embodiment is the inhibition ability of test inhibitor to ammonium chloride crystals salt.Add 100 gram refinery catalytic gasolines in tri-mouthfuls of Florence flasks of a 200mL, the character of catalytic gasoline is as shown in table 1, then add 1 gram chloride solid powder, slowly stir in 50 ℃ of water-baths, after stopping after 30 minutes stirring, observe the chloride solid powder deposition at drag.With dropper, to slowly dripping 1.5 gram proportionings in catalytic gasoline, be amino dodecane: rare five amine of tetrem: propyl carbinol: heavy aromatics=30: 35: 15: 20 inhibitor of the present invention, slowly stir and find that the chloride solid powder fades away, and observed bubble and overflowed in gasoline, stopped stirring the completely dissolve of discovery chloride solid powder after 5 minutes.
The character of table 1 catalytic gasoline
| Catalytic gasoline | Density, g/cm 3 | Sulphur, μ g/g | Nitrogen, μ g/g | Colloid, mg/100mL |
| Before inhibiting | 0.7224 | 502 | 185 | 1.5 |
| After inhibiting | 0.7226 | 498 | 1260 | 1.5 |
Certain refinery delayed coking unit, coking fractional distillation column often occurs that the top circular wave is larger, and top is followed the frequent discontinuity of pump and is found time, and the tower top temperature fluctuation is larger, and raw gasline is done rising, black.After salt crust appears in coking fractional distillation column, add salt coagulation inhibitor before the fractionator overhead pump entry, the proportioning of salt coagulation inhibitor is octodrine: amino dodecane: propyl carbinol: heavy aromatics=30: 30: 20: 20, and add-on is 40mg/kg, turn round after 36 hours, the separation column operation recovery is normal.The character of adding salt coagulation inhibitor front and back coker gasoline is as shown in table 2.
Table 2 adds the character of salt coagulation inhibitor front and back coker gasoline
| Catalytic gasoline | Density, g/cm 3 | Sulphur, μ g/g | Nitrogen, μ g/g | Colloid, mg/100mL |
| Before inhibiting | 0.7340 | 543 | 204 | 1.6 |
| After inhibiting | 0.7298 | 538 | 210 | 1.6 |
Embodiment 3
The salt coagulation of fractionating tower problem, often appear in certain refinery heavy oil catalytically cracking equipment, and plate pressure drop increases, and it is larger that gasoline products is done fluctuating range., after salt crust appears in catalytic cracking fractionating tower, at the trim the top of column line, add salt coagulation inhibitor, the salt coagulation inhibitor proportioning is amino dodecane: rare five amine of tetrem: propyl carbinol: heavy aromatics=30: 35: 15: 20, filling rate is 30mg/kg, and after turning round 45 hours, the separation column operation recovery is normal.The character of adding salt coagulation inhibitor front and back catalytic gasoline is as shown in table 3.
Table 3 adds the character of salt coagulation inhibitor front and back catalytic gasoline
| Catalytic gasoline | Density, g/cm 3 | Sulphur, μ g/g | Nitrogen, μ g/g | Colloid,, mg/100mL |
| Before inhibiting | 0.7218 | 482 | 178 | 1.5 |
| After inhibiting | 0.7215 | 475 | 183 | 1.5 |
Claims (9)
1. a technique of processing salt coagulation of fractionating tower, it is characterized in that: the trim the top of column pipeline at separation column adds a kind of salt coagulation inhibitor continuously, salt coagulation inhibitor with enter separation column after oil product in the trim the top of column pipeline mixes, 30～60mg/kg that the add-on of salt coagulation inhibitor is oil product flow in the trim the top of column pipeline, joining day is 30～60 hours, and wherein said salt coagulation inhibitor is comprised of following component:
(A) 30～70 % by weight fat nitrogenous compounds;
(B) 10～30 % by weight alkyl alcohols;
(C) 20～40 % by weight organic solvents;
In the salt coagulation inhibitor gross weight, described organic solvent is C
7～C
12any one or two kinds in aromatic hydrocarbons, described fatty nitrogenous compound is C
6～C
18any one in aliphatic amide or two kinds, alkyl alcohol is C
3～C
5any one or two kinds in alkyl monocarbon alcohol or dibasic alcohol.
2. technique according to claim 1, it is characterized in that: described fatty nitrogenous compound is C
8～C
12any one in aliphatic amide or two kinds.
3. technique according to claim 1, it is characterized in that: the content of described fatty nitrogenous compound is 50～65 % by weight, and the content of alkyl alcohol is 15～25 % by weight, and the content of organic solvent is 20～30 % by weight, in the salt coagulation inhibitor gross weight.
4. a technique of processing salt coagulation of fractionating tower, it is characterized in that: before the tower top pump entry of separation column, add continuously a kind of salt coagulation inhibitor, salt coagulation inhibitor with enter separation column after the oil product at tower top pump entry place mixes, 30～60mg/kg that the add-on of salt coagulation inhibitor is tower top pump entry place oil product flow, joining day is 30～60 hours, and wherein said salt coagulation inhibitor is comprised of following component:
(A) 30～70 % by weight fat nitrogenous compounds;
(B) 10～30 % by weight alkyl alcohols;
(C) 20～40 % by weight organic solvents;
In the salt coagulation inhibitor gross weight, described organic solvent is C
7～C
12any one or two kinds in aromatic hydrocarbons, described fatty nitrogenous compound is C
6～C
18any one in aliphatic amide or two kinds, alkyl alcohol is C
3～C
5any one or two kinds in alkyl monocarbon alcohol or dibasic alcohol.
5. technique according to claim 4, it is characterized in that: described fatty nitrogenous compound is C
8～C
12any one in aliphatic amide or two kinds.
6. technique according to claim 4, it is characterized in that: the content of described fatty nitrogenous compound is 50～65 % by weight, and the content of alkyl alcohol is 15～25 % by weight, and the content of organic solvent is 20～30 % by weight, in the salt coagulation inhibitor gross weight.
7. a technique of processing salt coagulation of fractionating tower, it is characterized in that: before the trim the top of column pipeline of separation column and tower top pump entry, add continuously a kind of salt coagulation inhibitor, salt coagulation inhibitor with enter separation column after the oil product at trim the top of column pipeline and tower top pump entry place mixes, 30～60mg/kg that the add-on of salt coagulation inhibitor is trim the top of column pipeline and tower top pump entry place oil product flow, joining day is 30～60 hours, and wherein said salt coagulation inhibitor is comprised of following component:
(A) 30～70 % by weight fat nitrogenous compounds;
(B) 10～30 % by weight alkyl alcohols;
(C) 20～40 % by weight organic solvents;
In the salt coagulation inhibitor gross weight, described organic solvent is C
7～C
12any one or two kinds in aromatic hydrocarbons, described fatty nitrogenous compound is C
6～C
18any one in aliphatic amide or two kinds, alkyl alcohol is C
3～C
5any one or two kinds in alkyl monocarbon alcohol or dibasic alcohol.
8. technique according to claim 7, it is characterized in that: described fatty nitrogenous compound is C
8～C
12any one in aliphatic amide or two kinds.
9. technique according to claim 7, it is characterized in that: the content of described fatty nitrogenous compound is 50～65 % by weight, and the content of alkyl alcohol is 15～25 % by weight, and the content of organic solvent is 20～30 % by weight, in the salt coagulation inhibitor gross weight.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010256526.8A CN102373066B (en) | 2010-08-19 | 2010-08-19 | Process for treating salt deposition in fractionating tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010256526.8A CN102373066B (en) | 2010-08-19 | 2010-08-19 | Process for treating salt deposition in fractionating tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102373066A CN102373066A (en) | 2012-03-14 |
| CN102373066B true CN102373066B (en) | 2014-01-08 |
Family
ID=45792303
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010256526.8A Active CN102373066B (en) | 2010-08-19 | 2010-08-19 | Process for treating salt deposition in fractionating tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102373066B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102703114A (en) * | 2012-05-28 | 2012-10-03 | 李小燕 | Method for preventing fractionating tower from salt deposition |
| CN103194258B (en) * | 2013-04-19 | 2014-10-22 | 华东理工大学 | Method for prolonging operation period of circulation oil system on top of fractionation tower |
| CN106701193B (en) * | 2015-07-27 | 2019-06-07 | 中国石油天然气股份有限公司 | A kind of fractionation tower top follows the anti-salt crust of system and opens a way online water washing device and method |
| CN107513400B (en) * | 2017-10-16 | 2020-01-10 | 中石化炼化工程（集团）股份有限公司 | Oil refining device anti-salt method, anti-salt system and application |
| CN108329942A (en) * | 2018-03-09 | 2018-07-27 | 山东京博石油化工有限公司 | A kind of device and technique of online processing salt crust |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1117989A (en) * | 1993-11-16 | 1996-03-06 | 中国石化广州石油化工总厂 | Method for improving corrosion of catalytically cracked gasoline |
| CN1754944A (en) * | 2004-09-29 | 2006-04-05 | 上海贵通新材料科技有限公司 | Corrosion inhibitor for hydrogenation plant |
| CN101440493A (en) * | 2008-12-17 | 2009-05-27 | 南京石油化工股份有限公司 | High temperature corrosion inhibitor for atmospheric vacuum distillation apparatus |
-
2010
- 2010-08-19 CN CN201010256526.8A patent/CN102373066B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1117989A (en) * | 1993-11-16 | 1996-03-06 | 中国石化广州石油化工总厂 | Method for improving corrosion of catalytically cracked gasoline |
| CN1754944A (en) * | 2004-09-29 | 2006-04-05 | 上海贵通新材料科技有限公司 | Corrosion inhibitor for hydrogenation plant |
| CN101440493A (en) * | 2008-12-17 | 2009-05-27 | 南京石油化工股份有限公司 | High temperature corrosion inhibitor for atmospheric vacuum distillation apparatus |
Non-Patent Citations (1)
| Title |
|---|
| 王新华，袁存昱，张海莹.焦化分馏塔结盐分析及可行性处理的探索.《安微化工》.2007,第33卷(第5期), * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102373066A (en) | 2012-03-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102373066B (en) | Process for treating salt deposition in fractionating tower | |
| KR101543499B1 (en) | Process for removing metals from vacuum gas oil | |
| CN103131472B (en) | Process method for delaying coking apparatus fractionation tower online salt washing | |
| CN104711008B (en) | A kind of device for preventing oil distillation column salt crust | |
| JP6739829B1 (en) | Separation apparatus and method for highly efficient purification treatment of waste oil residual liquid in chemical industry | |
| CN103555363B (en) | A kind of high containing acid starting material oil hydrogen supply delayed coking method | |
| CN204151295U (en) | A kind of anti-salt crust device of liquid-liquid extraction | |
| CN103194258B (en) | Method for prolonging operation period of circulation oil system on top of fractionation tower | |
| CN109384341A (en) | Semi-coke high concentrated organic wastewater recycling treatment system and method | |
| WO2014117310A1 (en) | Distillate two-phase hydrogenation reactor and hydrogenation process method | |
| CN102373067B (en) | Method for preventing salt coagulation of fractionating tower | |
| CN105647566A (en) | Fractionating system and method for reducing scaling and corrosion of fractionating system | |
| CN204151297U (en) | A kind of chlorion extracting corrosion-resisting device | |
| CN102373068B (en) | Salt coagulation inhibitor and preparation method thereof | |
| CN105295989A (en) | Dehydrating and desalinizing method of high-temperature coal tar | |
| CN206463528U (en) | Online washing fractionation tower top follows system | |
| CN110642314A (en) | Process unit for comprehensively utilizing crude oil electric desalting sewage by delayed coking device | |
| CN107880930B (en) | Energy-saving dirty oil dehydration device and treatment method thereof | |
| CN102659497B (en) | Water system of device for preparing olefins from methanol and on-line cleaning method thereof | |
| CN109880648B (en) | Fractionating tower circulating device and water washing method | |
| JPH01275692A (en) | Method of treating waste engine oil | |
| CN106701144B (en) | A kind of in-line purification method and its F- T synthesis system for F- T synthesis | |
| CN209178168U (en) | It is a kind of handle semi-coke high concentrated organic wastewater deamination mention phenol device | |
| CN110387257B (en) | Demetallizing agent suitable for demetallizing clear tank oil, composition thereof and method for treating clear tank oil | |
| CN206783601U (en) | A kind of F- T synthesis system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent for invention or patent application | ||
| CB02 | Change of applicant information |
Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: Sinopec Corp. Co-applicant after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: Sinopec Corp. Co-applicant before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |