CN106520184B - A kind of preparation method of high asphaltenes crude oil demulsifier - Google Patents
A kind of preparation method of high asphaltenes crude oil demulsifier Download PDFInfo
- Publication number
- CN106520184B CN106520184B CN201611068448.2A CN201611068448A CN106520184B CN 106520184 B CN106520184 B CN 106520184B CN 201611068448 A CN201611068448 A CN 201611068448A CN 106520184 B CN106520184 B CN 106520184B
- Authority
- CN
- China
- Prior art keywords
- added
- demulsifier
- warming
- added dropwise
- temperature
- 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
- 239000010779 crude oil Substances 0.000 title claims abstract description 23
- 238000002360 preparation method Methods 0.000 title claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 57
- 238000010792 warming Methods 0.000 claims abstract description 55
- 238000007664 blowing Methods 0.000 claims abstract description 31
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000005086 pumping Methods 0.000 claims abstract description 20
- 239000003999 initiator Substances 0.000 claims abstract description 17
- QWXYZCJEXYQNEI-OSZHWHEXSA-N intermediate I Chemical compound COC(=O)[C@@]1(C=O)[C@H]2CC=[N+](C\C2=C\C)CCc2c1[nH]c1ccccc21 QWXYZCJEXYQNEI-OSZHWHEXSA-N 0.000 claims abstract description 17
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000003054 catalyst Substances 0.000 claims abstract description 11
- WBIQQQGBSDOWNP-UHFFFAOYSA-N 2-dodecylbenzenesulfonic acid Chemical compound CCCCCCCCCCCCC1=CC=CC=C1S(O)(=O)=O WBIQQQGBSDOWNP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229940060296 dodecylbenzenesulfonic acid Drugs 0.000 claims abstract description 9
- GSEJCLTVZPLZKY-UHFFFAOYSA-N Triethanolamine Chemical compound OCCN(CCO)CCO GSEJCLTVZPLZKY-UHFFFAOYSA-N 0.000 claims abstract description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 87
- 238000003756 stirring Methods 0.000 claims description 31
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 claims description 26
- 238000010438 heat treatment Methods 0.000 claims description 22
- 230000018044 dehydration Effects 0.000 claims description 21
- 238000006297 dehydration reaction Methods 0.000 claims description 21
- 239000007788 liquid Substances 0.000 claims description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 20
- 239000000243 solution Substances 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- SXRSQZLOMIGNAQ-UHFFFAOYSA-N Glutaraldehyde Chemical compound O=CCCCC=O SXRSQZLOMIGNAQ-UHFFFAOYSA-N 0.000 claims description 12
- 238000010992 reflux Methods 0.000 claims description 12
- 208000005156 Dehydration Diseases 0.000 claims description 10
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- RVGRUAULSDPKGF-UHFFFAOYSA-N Poloxamer Chemical compound C1CO1.CC1CO1 RVGRUAULSDPKGF-UHFFFAOYSA-N 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 8
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 claims description 7
- 238000004321 preservation Methods 0.000 claims description 7
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 claims description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 238000002844 melting Methods 0.000 claims description 6
- 230000008018 melting Effects 0.000 claims description 6
- 238000003786 synthesis reaction Methods 0.000 claims description 6
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 5
- 229910052708 sodium Inorganic materials 0.000 claims description 5
- 239000011734 sodium Substances 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- 239000001257 hydrogen Substances 0.000 claims description 4
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 4
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 claims description 4
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 claims description 4
- 229910001948 sodium oxide Inorganic materials 0.000 claims description 4
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 claims description 4
- -1 potassium ferricyanide Iron zinc Chemical compound 0.000 claims description 3
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 claims description 2
- 239000004593 Epoxy Substances 0.000 claims description 2
- 239000007864 aqueous solution Substances 0.000 claims description 2
- 239000002738 chelating agent Substances 0.000 claims description 2
- 239000001301 oxygen Substances 0.000 claims description 2
- 229910052760 oxygen Inorganic materials 0.000 claims description 2
- 235000005074 zinc chloride Nutrition 0.000 claims description 2
- 239000011592 zinc chloride Substances 0.000 claims description 2
- YWOITFUKFOYODT-UHFFFAOYSA-N methanol;sodium Chemical compound [Na].OC YWOITFUKFOYODT-UHFFFAOYSA-N 0.000 claims 1
- 239000000839 emulsion Substances 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 4
- KIDXYAWWICJAFK-UHFFFAOYSA-N O.[Na].OC Chemical compound O.[Na].OC KIDXYAWWICJAFK-UHFFFAOYSA-N 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 4
- GRONZTPUWOOUFQ-UHFFFAOYSA-M sodium;methanol;hydroxide Chemical compound [OH-].[Na+].OC GRONZTPUWOOUFQ-UHFFFAOYSA-M 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000010426 asphalt Substances 0.000 description 2
- ZZVUWRFHKOJYTH-UHFFFAOYSA-N diphenhydramine Chemical compound C=1C=CC=CC=1C(OCCN(C)C)C1=CC=CC=C1 ZZVUWRFHKOJYTH-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000011295 pitch Substances 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000001934 delay Effects 0.000 description 1
- CASPZMCSNJZQMV-UHFFFAOYSA-N ethane;2-methyloxirane Chemical compound CC.CC1CO1 CASPZMCSNJZQMV-UHFFFAOYSA-N 0.000 description 1
- 235000019441 ethanol Nutrition 0.000 description 1
- KFZAUHNPPZCSCR-UHFFFAOYSA-N iron zinc Chemical compound [Fe].[Zn] KFZAUHNPPZCSCR-UHFFFAOYSA-N 0.000 description 1
- 239000006210 lotion Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000009671 shengli Substances 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 238000010189 synthetic method Methods 0.000 description 1
- 238000011282 treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G33/00—Dewatering or demulsification of hydrocarbon oils
- C10G33/04—Dewatering or demulsification of hydrocarbon oils with chemical means
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
- C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
- C08G65/2603—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen
- C08G65/2606—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen containing hydroxyl groups
- C08G65/2612—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen containing hydroxyl groups containing aromatic or arylaliphatic hydroxyl groups
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of preparation method of high asphaltenes crude oil demulsifier, wherein the specific steps are as follows: 1) by phenol, toluene in 1:(1.3-1.6) ratio be added in reaction kettle, addition dmc catalyst；2) initiator obtained by step 1), demulsifier intermediate I, demulsifier intermediate II pumping are added to reaction kettle, pumping adds 50% sodium hydrate methanol solution；3) dodecyl benzene sulfonic acid is added in reaction kettle, triethanolamine is added dropwise from dropping tank；4) intermediate III and intermediate IV are added in reaction kettle by the weight ratio of 17:(2-3), are warming up to 50 DEG C of blowings, obtain high asphaltenes crude oil demulsifier；Advantage are as follows: the invention problem slow for high asphaltenes crude oil demulsification initial stage dewatering speed, the high molecular weight demulsifier containing a large amount of branches is synthesized, initial stage breaking emulsion and dewatering speed can be substantially improved, being aided with intermediate B can ensure that final dewatering rate reaches 90% or more simultaneously, with with strong points, the characteristics of dewatering speed is fast and excellent effect.
Description
Technical field
The present invention relates to a kind of synthetic method of high molecular material, especially a kind of high asphaltenes crude oil demulsifier
Preparation method belongs to oil field mining liquid chemical treatments preparation field.
Background technique
There is a large amount of viscous crude resource reserve in China, is concentrated mainly on the oil fields such as Shengli Oil Field, Liaohe Oil Field, Dagang Oilfield,
Colloid, asphalt content are very high in viscous crude.Though asphalitine surface-active is weak, when asphalitine content in crude oil is more than
Crude oil will be made to form stable emulsion when 1000ppm, as the increase of asphalt content can also be formed in oil-water interfaces layer
Stable film prevents the water droplet in emulsion from gathering and settle, so that influencing demulsifier plays effect.Current research is thought in viscous crude
Asphalitine be to assemble to form stable emulsion in oil-water interfaces in the form of rigid cross-linked network, and the thinking of this patent
It is to control transfer of the asphalitine to interface using branch a large amount of in demulsifier, to reduce interface film strength to reach and increase
The purpose of strong demulsifier effect.According to asphalitine characteristic and the thinking of control pitch transfer, we targetedly develop one kind
High asphaltenes crude oil demulsifier.
Summary of the invention
The purpose of the present invention is to solve contain a large amount of pitches in viscous crude to cause oil-water interfaces film-strength to increase, in lotion
Water droplet can not gather and settle, and causing general demulsifier to be demulsified in viscous crude, difficult, initial dewatering speed is slow, abjection water middle layer is existing
A kind of preparation method for high asphaltenes crude oil demulsifier proposed as the disadvantages of serious, dehydration rate is not up to standard.
The technical scheme adopted by the invention is that: a kind of preparation method of high asphaltenes crude oil demulsifier, it is described
The specific steps of preparation method are as follows:
1) be in mass ratio 1:(1.3-1.6 by phenol, toluene) ratio be added in reaction kettle, be added phenol quality
1.5 ‰ ~ 2.0 ‰ dmc catalyst, described in dmc catalyst be the aqueous solution for containing chelating agent with zinc chloride, the potassium ferricyanide
For the iron zinc bimetallic cyanide complex catalyst of raw material, it is warming up to 60 DEG C and is stirred 30 minutes after product melting, open drop
Add tank valve that glutaraldehyde is slowly added dropwise, the amount that glutaraldehyde is added is 1 ~ 1.2 times of phenol amount, controls temperature at 60 DEG C ~ 70 DEG C, drips
It is warming up to 80 DEG C ~ 85 DEG C after adding and keeps the temperature 3 hours, heat preservation finishes cooling for reflux system of opening, and heating carries out reflux dewatering, delays
Slow heating is finally warming up to 160 DEG C ~ 165 DEG C, is kept for 2 hours at such a temperature, during which return tank water level, which remains stationary, is considered as water
Divide and take off, moisture is cooled to 100 DEG C of blowings and obtains initiator after taking off；
2) pumping of initiator obtained by step 1) is added in reaction kettle, takes out 3.6% or 5% 50% hydrogen for adding initiator quality
Sodium oxide molybdena methanol solution, stirs evenly, and is steadily warming up to 110 DEG C ~ 120 DEG C, opens vacuum valve and carries out vacuum dehydration, will be in raw material
Water and methanol abjection, keep vacuum 2 hours to no liquid to deviate from, close vacuum valve, then with nitrogen by pressure balance in kettle
To 0.00MPa, 115 DEG C ~ 125 DEG C are then steadily warming up to, 5 ~ 7 times of initiator quality of propylene oxide, control are added dropwise in proportion
120 DEG C ~ 125 DEG C of reaction temperature, 1.5 hours are kept the temperature at 115 DEG C ~ 125 DEG C after being added dropwise, it is standby to obtain demulsifier intermediate I blowing
With；
3) demulsifier intermediate I pumping is added in reaction kettle, takes out the 50% of the quality 18% or 22% for adding demulsifier intermediate I
Sodium hydrate methanol solution, stir evenly, be warming up to 110 ~ 120 DEG C of unlatching vacuum valves and carry out vacuum dehydrations, keep vacuum 2 small
Deviate from up to no liquid, closes vacuum valve, pressure balance in kettle to 0.00MPa is then continuously heating to 120 ~ 125 with nitrogen
DEG C, the ethylene oxide propylene oxide mixture of 31 ~ 36 times of demulsifier intermediate I quality, ethylene oxide epoxy third are added dropwise in proportion
Alkane mixture ratio mass ratio is 1:1.5, keeps reaction temperature between 120 DEG C ~ 125 DEG C, at 120 ~ 125 DEG C after being added dropwise
Heat preservation 1.5 hours, it is spare to obtain demulsifier intermediate II blowing；
4) demulsifier intermediate II pumping is added in reaction kettle, takes out the 50% of the quality 3% or 5% for adding demulsifier intermediate II
Sodium hydrate methanol solution, stir evenly, be warming up to 110 DEG C ~ 120 DEG C unlatching vacuum valves and carry out vacuum dehydrations, keep vacuum 2
Hour to no liquid is deviate from, and closes vacuum valve, pressure balance in kettle to 0.00MPa is then continuously heating to 115 DEG C with nitrogen
~ 120 DEG C, in proportion be added dropwise 5.5 ~ 6.5 times of demulsifier intermediate II quality ethylene oxide, control reaction temperature be 120 DEG C ~
125 DEG C, 120 DEG C ~ 125 DEG C of temperature are kept after being added dropwise and keeps the temperature 1.5 hours, blowing obtains intermediate III；
5) dodecyl benzene sulfonic acid is added in reaction kettle, is warming up to 50 DEG C, triethanolamine is slowly added dropwise from dropping tank,
Temperature≤65 DEG C are controlled, wherein triethanolamine and dodecyl benzene sulfonic acid mass ratio are 1:(2-2.5), 30 are stirred after being added dropwise
Minute, 45 DEG C are cooled to, methanol and isopropanol is added, solid content is adjusted to 50%, methanol and isopropanol mass ratio are 3:(1-
1.5) it, stirs 60 minutes, obtains intermediate IV；
6) intermediate III and intermediate IV are added in reaction kettle by weight the ratio for 17:(2-3), are warming up to
It 50 DEG C, stirs 30 minutes, blowing, product synthesis finishes, and obtains high asphaltenes crude oil demulsifier.
The preferred plan of the preparation method are as follows:
1) 1 part of phenol, 1.4 parts of toluene are added in reaction kettle, 0.0015 part of dmc catalyst is added, is warming up to 60 DEG C
It is stirred 30 minutes after product melting, opens dropwise addition tank valve and glutaraldehyde is slowly added dropwise, the amount that glutaraldehyde is added is 1 part, control
Temperature is warming up to 80 DEG C ~ 85 DEG C and keeps the temperature 3 hours at 60 DEG C ~ 70 DEG C after being added dropwise, heat preservation, which finishes, opens cooling for reflux system,
Heating carries out reflux dewatering, and slowly heating is finally warming up to 160 DEG C ~ 165 DEG C, at such a temperature holding 2 hours, during which return tank
Water level, which remains stationary, to be considered as moisture and takes off, and moisture is cooled to 100 DEG C of blowings and obtains initiator after taking off；
2) 1 part of initiator pumping obtained by step 1) is added in reaction kettle, takes out the hydroxide for adding 0.036 part of mass ratio to be 50%
The methanol solution of sodium, stirs evenly, and is steadily warming up to 110 DEG C ~ 120 DEG C, opens vacuum valve and carries out vacuum dehydration, will be in raw material
Water and methanol abjection, keep vacuum 2 hours to no liquid to deviate from, and close vacuum valve nitrogen for pressure balance in kettle extremely
Then 0.00MPa is steadily warming up to 115 DEG C ~ 125 DEG C, 6 parts of propylene oxide are added dropwise, and controls 120 DEG C ~ 125 DEG C of reaction temperature, drop
1.5 hours are kept the temperature at 115 DEG C ~ 125 DEG C after adding, it is spare to obtain demulsifier intermediate I blowing；
3) 1 part of intermediate I pumping of demulsifier obtained by step 2 is added in reaction kettle, takes out the hydrogen for adding 0.18 mass ratio to be 50%
The methanol solution of sodium oxide molybdena, stirs evenly, and is warming up to 110 ~ 120 DEG C of unlatching vacuum valves and carries out vacuum dehydration, is kept for vacuum 2 hours
Deviate to no liquid, closes vacuum valve for pressure balance in kettle to 0.00MPa, be continuously heating to 120 ~ 125 DEG C, 32 parts of rings are added dropwise
Oxidative ethane propylene oxide mixture, ethylene oxide propylene oxide ratio be (2:3), keep reaction temperature 120 DEG C ~ 125 DEG C it
Between, 1.5 hours are kept the temperature at 120 ~ 125 DEG C after being added dropwise, it is spare to obtain demulsifier intermediate II blowing；
4) 1 part of intermediate II pumping of demulsifier obtained by step 3) is added in reaction kettle, smokes plus 0.03 part of mass ratio is 50%
The methanol solution of sodium hydroxide, stirs evenly, and is warming up to 110 DEG C ~ 120 DEG C unlatching vacuum valves and carries out vacuum dehydration, keeps vacuum 2
Hour to no liquid is deviate from, and is closed vacuum valve for pressure balance in kettle to 0.00MPa, is continuously heating to 115 DEG C ~ 120 DEG C, is added dropwise
5.5 parts of ethylene oxide, control reaction temperature are 120 DEG C ~ 125 DEG C, keep 120 DEG C ~ 125 DEG C of temperature to keep 1.5 after being added dropwise
Hour, blowing obtains intermediate III；
5) 1 part of dodecyl benzene sulfonic acid is added in reaction kettle, is warming up to 50 DEG C, three ethyl alcohol are slowly added dropwise from dropping tank
2 parts of amine, temperature≤65 DEG C are controlled, are stirred 30 minutes after being added dropwise, be cooled to 45 DEG C, methanol and isopropyl alcohol mixture is added
3 parts, solid content is adjusted to 50%, methanol and isopropanol mass ratio are 3:1, stir 60 minutes, obtain intermediate IV；
6) intermediate III and intermediate IV are added in reaction kettle for the ratio of 8:1 in mass ratio, are warming up to 50 DEG C, stir
It mixes 30 minutes, blowing, product synthesis finishes, and obtains high asphaltenes crude oil demulsifier.
The main physico-chemical parameter of the demulsifier are as follows:
Appearance: the sticky uniform liquid of buff, no mechanical admixture；
PH value: 7 ~ 8；
Flash-point: >=25 DEG C；
Solid content: >=95%；
Relative dehydration rate: >=90%.
The chemical equation that the preparation method is related to are as follows:
Remarks: a=a1+a2+a3+a4;b=b1+b2+b3+b4;
c=c1+c2+c3+c4。
The beneficial effects of the present invention are: a kind of preparation method of high asphaltenes crude oil demulsifier is directed to emphatically height containing drip
The slow problem of green matter crude oil demulsification initial stage dewatering speed, has synthesized the high molecular weight demulsifier containing a large amount of branches, can be substantially improved
Initial stage breaking emulsion and dewatering speed, while being aided with intermediate B and can ensure that final dewatering rate reaches at least 90% or more, have it is with strong points,
The characteristics of dewatering speed is fast and excellent effect.
Specific embodiment
Embodiment 1:
1) phenol 100Kg, toluene 140Kg are added in reaction kettle, 0.15KgDMC catalyst is added, is warming up to 60 DEG C
It is stirred 30 minutes after product melting, opens dropwise addition tank valve and glutaraldehyde is slowly added dropwise, the amount that glutaraldehyde is added is 100Kg, control
Temperature processed is warming up to 80 DEG C ~ 85 DEG C and keeps the temperature 3 hours at 60 DEG C ~ 70 DEG C after being added dropwise, heat preservation, which finishes, opens cooling for reflux system
System, heating carry out reflux dewatering, and slowly heating is finally warming up to 160 DEG C ~ 165 DEG C, is kept for 2 hours, is during which returned at such a temperature
Stream tank water level, which remains stationary, to be considered as moisture and takes off, and moisture is cooled to 100 DEG C of blowings and obtains initiator after taking off.
2) pumping of initiator 100Kg obtained by step 1) is added in reaction kettle, takes out the hydrogen-oxygen for adding 3.6Kg mass fraction to be 50%
The methanol solution for changing sodium, stirs evenly, and is steadily warming up to 110 DEG C ~ 120 DEG C, opens vacuum valve and carries out vacuum dehydration, will be in raw material
Water and methanol abjection, keep vacuum 2 hours to no liquid to deviate from, close vacuum valve nitrogen for pressure balance in kettle extremely
Then 0.00MPa is steadily warming up to 115 DEG C ~ 125 DEG C, 600Kg propylene oxide is added dropwise, and controls 120 DEG C ~ 125 DEG C of reaction temperature,
1.5 hours are kept the temperature at 115 DEG C ~ 125 DEG C after being added dropwise, it is spare to obtain demulsifier intermediate I blowing.
3) pumping of demulsifier intermediate I 100Kg obtained by step 2 is added in reaction kettle, takes out plus 18Kg mass fraction is 50%
Sodium hydroxide methanol solution, stir evenly, be warming up to 110 ~ 120 DEG C of unlatching vacuum valves and carry out vacuum dehydrations, keep vacuum 2
Hour to no liquid is deviate from, and is closed vacuum valve for pressure balance in kettle to 0.00MPa, is continuously heating to 120 ~ 125 DEG C, is added dropwise
3200Kg ethylene oxide propylene oxide mixture, ethylene oxide propylene oxide ratio are (1280Kg:1920Kg), keep reaction temperature
Degree keeps the temperature 1.5 hours at 120 ~ 125 DEG C after being added dropwise, it is standby to obtain demulsifier intermediate II blowing between 120 DEG C ~ 125 DEG C
With.
4) pumping of demulsifier intermediate II 100Kg obtained by step 3) is added in reaction kettle, takes out plus 3Kg mass fraction is 50%
Sodium hydroxide methanol solution, stir evenly, be warming up to 110 DEG C ~ 120 DEG C unlatching vacuum valves and carry out vacuum dehydrations, keep true
Deviate to no liquid within empty 2 hours, close vacuum valve for pressure balance in kettle to 0.00MPa, be continuously heating to 115 DEG C ~ 120 DEG C,
550Kg ethylene oxide is added dropwise, control reaction temperature is 120 DEG C ~ 125 DEG C, and 120 DEG C ~ 125 DEG C of temperature holdings are kept after being added dropwise
1.5 hours, blowing obtained intermediate III.
5) 100Kg dodecyl benzene sulfonic acid is added in reaction kettle, is warming up to 50 DEG C, three second are slowly added dropwise from dropping tank
Hydramine 200Kg controls temperature≤65 DEG C, stirs 30 minutes after being added dropwise, and is cooled to 45 DEG C, and methanol and isopropanol mixing is added
Solid content is adjusted to 50% by solution 300Kg, and methanol and isopropanol mass ratio are 225Kg:75Kg, stir 60 minutes, obtain centre
Body IV.
6) intermediate A 160Kg and intermediate B 20Kg are added in reaction kettle, are warming up to 50 DEG C, stirred 30 minutes,
Blowing, product synthesis finish, and obtain high asphaltenes crude oil demulsifier.
Embodiment 2:
1) phenol 100Kg, toluene 160Kg are added in reaction kettle, be added 0.2KgDMC catalyst, be warming up to 60 DEG C to
It is stirred 30 minutes after product melting, opens dropwise addition tank valve and glutaraldehyde is slowly added dropwise, glutaraldehyde 120Kg is added, control temperature exists
60 DEG C ~ 70 DEG C, be warming up to after being added dropwise 80 DEG C ~ 85 DEG C keep the temperature 3 hours, heat preservation finish open cooling for reflux system, heat up into
Row reflux dewatering, slowly heating is finally warming up to 160 DEG C ~ 165 DEG C, keeps at such a temperature 2 hours, during which return tank water level is protected
It holds the motionless moisture that is considered as to take off, moisture is cooled to 100 DEG C of blowings and obtains initiator after taking off.
2) pumping of initiator 100Kg obtained by step 1) is added in reaction kettle, takes out the hydroxide for adding 5Kg mass fraction to be 50%
The methanol solution of sodium, stirs evenly, and is steadily warming up to 110 DEG C ~ 120 DEG C, opens vacuum valve and carries out vacuum dehydration, will be in raw material
Water and methanol abjection, keep vacuum 2 hours to no liquid to deviate from, and close vacuum valve nitrogen for pressure balance in kettle extremely
Then 0.00MPa is steadily warming up to 115 DEG C ~ 125 DEG C, 700Kg propylene oxide is added dropwise, and controls 120 DEG C ~ 125 DEG C of reaction temperature,
1.5 hours are kept the temperature at 115 DEG C ~ 125 DEG C after being added dropwise, it is spare to obtain demulsifier intermediate I blowing.
3) pumping of demulsifier intermediate I 100Kg obtained by step 2 is added in reaction kettle, takes out plus 22Kg mass fraction is 50%
Sodium hydroxide methanol solution, stir evenly, be warming up to 110 ~ 120 DEG C of unlatching vacuum valves and carry out vacuum dehydrations, keep vacuum 2
Hour to no liquid is deviate from, and is closed vacuum valve for pressure balance in kettle to 0.00MPa, is continuously heating to 120 ~ 125 DEG C, is added dropwise
3600Kg ethylene oxide propylene oxide mixture, ethylene oxide propylene oxide ratio are (1440Kg:2160Kg), keep reaction temperature
Degree keeps the temperature 1.5 hours at 120 ~ 125 DEG C after being added dropwise, it is standby to obtain demulsifier intermediate II blowing between 120 DEG C ~ 125 DEG C
With.
4) pumping of demulsifier intermediate II 100Kg obtained by step 3) is added in reaction kettle, takes out plus 5Kg mass fraction is 50%
Sodium hydroxide methanol solution, stir evenly, be warming up to 110 DEG C ~ 120 DEG C unlatching vacuum valves and carry out vacuum dehydrations, keep true
Deviate to no liquid within empty 2 hours, close vacuum valve for pressure balance in kettle to 0.00MPa, be continuously heating to 115 DEG C ~ 120 DEG C,
650Kg ethylene oxide is added dropwise, control reaction temperature is 120 DEG C ~ 125 DEG C, and 120 DEG C ~ 125 DEG C of temperature holdings are kept after being added dropwise
1.5 hours, blowing obtained intermediate III.
5) 100Kg dodecyl benzene sulfonic acid is added in reaction kettle, is warming up to 50 DEG C, three second are slowly added dropwise from dropping tank
Hydramine 250Kg controls temperature≤65 DEG C, stirs 30 minutes after being added dropwise, and is cooled to 45 DEG C, and methanol and isopropanol mixing is added
Solid content is adjusted to 50% by solution 350Kg, and methanol and isopropanol mass ratio are 262Kg:88Kg, stir 60 minutes, obtain centre
Body IV.
6) intermediate A 160Kg and intermediate B 30Kg are added in reaction kettle, are warming up to 50 DEG C, stirred 30 minutes,
Blowing, product synthesis finish, and obtain high asphaltenes crude oil demulsifier.
Claims (4)
1. a kind of preparation method of high asphaltenes crude oil demulsifier, it is characterised in that:
The specific steps of the preparation method are as follows:
1) be in mass ratio 1:(1.3-1.6 by phenol, toluene) ratio be added in reaction kettle, be added phenol quality 1.5 ‰ ~
2.0 ‰ dmc catalyst, described in dmc catalyst be that the aqueous solution of chelating agent contained as raw material using zinc chloride, the potassium ferricyanide
Iron zinc bimetallic cyanide complex catalyst, be warming up to 60 DEG C after product melting after stir 30 minutes, open dropwise addition pot valve
Glutaraldehyde is slowly added dropwise in door, and the amount that glutaraldehyde is added is 1 ~ 1.2 times of phenol amount, controls temperature at 60 DEG C ~ 70 DEG C, is added dropwise
After be warming up to 80 DEG C ~ 85 DEG C keep the temperature 3 hours, heat preservation finish open cooling for reflux system, heating carry out reflux dewatering, slowly heat up
160 DEG C ~ 165 DEG C finally are warming up to, is kept at such a temperature 2 hours, during which return tank water level, which remains stationary, is considered as moisture and takes off,
Moisture is cooled to 100 DEG C of blowings and obtains initiator after taking off；
2) pumping of initiator obtained by step 1) is added in reaction kettle, takes out 3.6% or 5% 50% hydroxide for adding initiator quality
Sodium methanol solution, stirs evenly, and is steadily warming up to 110 DEG C ~ 120 DEG C, opens vacuum valve and carries out vacuum dehydration, by the water in raw material
Deviate from methanol, keep vacuum 2 hours to no liquid to deviate from, close vacuum valve, then with nitrogen by pressure balance in kettle extremely
Then 0.00MPa is steadily warming up to 115 DEG C ~ 125 DEG C, 5 ~ 7 times of initiator quality of propylene oxide is added dropwise in proportion, and control is anti-
120 DEG C ~ 125 DEG C of temperature are answered, 1.5 hours is kept the temperature at 115 DEG C ~ 125 DEG C after being added dropwise, it is spare to obtain demulsifier intermediate I blowing；
3) demulsifier intermediate I pumping is added in reaction kettle, takes out 50% hydrogen for adding the quality 18% or 22% of demulsifier intermediate I
Sodium oxide molybdena methanol solution, stirs evenly, and is warming up to 110 ~ 120 DEG C of unlatching vacuum valves and carries out vacuum dehydration, keeps vacuum 2 hours extremely
No liquid abjection, closes vacuum valve, pressure balance in kettle to 0.00MPa is then continuously heating to 120 ~ 125 DEG C with nitrogen,
The ethylene oxide propylene oxide mixture of 31 ~ 36 times of demulsifier intermediate I quality is added dropwise in proportion, ethylene oxide propylene oxide is mixed
Complex ratios mass ratio is 1:1.5, keeps reaction temperature between 120 DEG C ~ 125 DEG C, is kept the temperature after being added dropwise at 120 ~ 125 DEG C
1.5 hours, it is spare to obtain demulsifier intermediate II blowing；
4) demulsifier intermediate II pumping is added in reaction kettle, takes out 50% hydrogen for adding the quality 3% or 5% of demulsifier intermediate II
Sodium oxide molybdena methanol solution, stirs evenly, and is warming up to 110 DEG C ~ 120 DEG C unlatching vacuum valves and carries out vacuum dehydration, is kept for vacuum 2 hours
Deviate to no liquid, closes vacuum valve, pressure balance in kettle to 0.00MPa is then continuously heating to 115 DEG C ~ 120 with nitrogen
DEG C, the ethylene oxide of 5.5 ~ 6.5 times of demulsifier intermediate II quality is added dropwise in proportion, control reaction temperature is 120 DEG C ~ 125 DEG C,
120 DEG C ~ 125 DEG C of temperature are kept after being added dropwise and keeps the temperature 1.5 hours, and blowing obtains intermediate III；
5) dodecyl benzene sulfonic acid is added in reaction kettle, is warming up to 50 DEG C, triethanolamine is slowly added dropwise from dropping tank, controlled
Temperature≤65 DEG C, wherein triethanolamine and dodecyl benzene sulfonic acid mass ratio are 1:(2-2.5), 30 points are stirred after being added dropwise
Clock is cooled to 45 DEG C, and methanol and isopropanol is added, and solid content is adjusted to 50%, methanol and isopropanol mass ratio are 3:(1-1.5),
Stirring 60 minutes, obtains intermediate IV；
6) intermediate III and intermediate IV are added in reaction kettle by weight the ratio for 17:(2-3), are warming up to 50 DEG C,
Stirring 30 minutes, blowing, product synthesis finish, and obtain high asphaltenes crude oil demulsifier.
2. a kind of preparation method of high asphaltenes crude oil demulsifier according to claim 1, it is characterised in that:
The preferred plan of the preparation method are as follows:
1) 1 part of phenol, 1.4 parts of toluene are added in reaction kettle, 0.0015 part of dmc catalyst is added, be warming up to 60 DEG C wait produce
It is stirred 30 minutes after product melting, opens dropwise addition tank valve and glutaraldehyde is slowly added dropwise, the amount that glutaraldehyde is added is 1 part, controls temperature
At 60 DEG C ~ 70 DEG C, it is warming up to 80 DEG C ~ 85 DEG C after being added dropwise and keeps the temperature 3 hours, heat preservation finishes cooling for reflux system of opening, heating
Reflux dewatering is carried out, slowly heating is finally warming up to 160 DEG C ~ 165 DEG C, at such a temperature holding 2 hours, during which return tank water level
It remains stationary and is considered as moisture and takes off, moisture is cooled to 100 DEG C of blowings and obtains initiator after taking off；
2) 1 part of initiator pumping obtained by step 1) is added in reaction kettle, takes out the sodium hydroxide for adding 0.036 part of mass ratio to be 50%
Methanol solution stirs evenly, and is steadily warming up to 110 DEG C ~ 120 DEG C, opens vacuum valve and carries out vacuum dehydration, by raw material water and
Methanol abjection, keeps deviating to no liquid for vacuum 2 hours, closes vacuum valve nitrogen by pressure balance in kettle to 0.00MPa, so
Steadily be warming up to 115 DEG C ~ 125 DEG C afterwards, be added dropwise 6 parts of propylene oxide, control 120 DEG C ~ 125 DEG C of reaction temperature, after being added dropwise
115 DEG C ~ 125 DEG C keep the temperature 1.5 hours, and it is spare to obtain demulsifier intermediate I blowing；
3) 1 part of intermediate I pumping of demulsifier obtained by step 2 is added in reaction kettle, takes out the hydroxide for adding 0.18 mass ratio to be 50%
The methanol solution of sodium, stirs evenly, and is warming up to 110 ~ 120 DEG C of unlatching vacuum valves and carries out vacuum dehydrations, keeps vacuum 2 hours to nothing
Liquid abjection closes vacuum valve for pressure balance in kettle to 0.00MPa, is continuously heating to 120 ~ 125 DEG C, 32 parts of epoxy second are added dropwise
Alkane propylene oxide mixture, ethylene oxide propylene oxide ratio are (2:3), keep reaction temperature between 120 DEG C ~ 125 DEG C, drop
1.5 hours are kept the temperature at 120 ~ 125 DEG C after adding, it is spare to obtain demulsifier intermediate II blowing；
4) 1 part of intermediate II pumping of demulsifier obtained by step 3) is added in reaction kettle, takes out the hydrogen-oxygen for adding 0.03 part of mass ratio to be 50%
The methanol solution for changing sodium, stirs evenly, and is warming up to 110 DEG C ~ 120 DEG C unlatching vacuum valves and carries out vacuum dehydration, is kept for vacuum 2 hours
Deviate to no liquid, closes vacuum valve for pressure balance in kettle to 0.00MPa, be continuously heating to 115 DEG C ~ 120 DEG C, be added dropwise 5.5
Part ethylene oxide, control reaction temperature are 120 DEG C ~ 125 DEG C, keep 120 DEG C ~ 125 DEG C of temperature holdings 1.5 small after being added dropwise
When, blowing obtains intermediate III；
5) 1 part of dodecyl benzene sulfonic acid is added in reaction kettle, is warming up to 50 DEG C, triethanolamine 2 is slowly added dropwise from dropping tank
Part, temperature≤65 DEG C are controlled, are stirred 30 minutes after being added dropwise, are cooled to 45 DEG C, methanol and isopropyl alcohol mixture 3 is added
Part, solid content is adjusted to 50%, methanol and isopropanol mass ratio are 3:1, stir 60 minutes, obtain intermediate IV；
6) intermediate III and intermediate IV are added in reaction kettle for the ratio of 8:1 in mass ratio, are warming up to 50 DEG C, stirring 30
Minute, blowing, product synthesis finishes, and obtains high asphaltenes crude oil demulsifier.
3. a kind of preparation method of high asphaltenes crude oil demulsifier according to claim 1, it is characterised in that:
The main physico-chemical parameter of the demulsifier are as follows:
Appearance: the sticky uniform liquid of buff, no mechanical admixture；
PH value: 7 ~ 8；
Flash-point: >=25 DEG C；
Solid content: >=95%；
Relative dehydration rate: >=90%.
4. a kind of preparation method of high asphaltenes crude oil demulsifier according to claim 1, it is characterised in that:
The chemical equation that the preparation method is related to are as follows:
Remarks: a=a1+a2+a3+a4； b=b1+b2+b3+b4；
c=c1+c2+c3+c4。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611068448.2A CN106520184B (en) | 2016-11-29 | 2016-11-29 | A kind of preparation method of high asphaltenes crude oil demulsifier |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611068448.2A CN106520184B (en) | 2016-11-29 | 2016-11-29 | A kind of preparation method of high asphaltenes crude oil demulsifier |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106520184A CN106520184A (en) | 2017-03-22 |
| CN106520184B true CN106520184B (en) | 2019-05-14 |
Family
ID=58353514
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611068448.2A Active CN106520184B (en) | 2016-11-29 | 2016-11-29 | A kind of preparation method of high asphaltenes crude oil demulsifier |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106520184B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108085055B (en) * | 2018-01-03 | 2021-03-30 | 德仕能源科技集团股份有限公司 | Method for preparing condensate oil water emulsion demulsifier by using phenol as raw material |
| CN108165302B (en) * | 2018-01-03 | 2020-09-11 | 德仕能源科技集团股份有限公司 | Preparation method of demulsifying agent for condensate oil-water emulsion |
| CN113428938A (en) * | 2021-07-23 | 2021-09-24 | 南通沃森环保科技有限公司 | Production process of wastewater demulsifier |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3223692A1 (en) * | 1982-06-25 | 1983-12-29 | Hoechst Ag, 6230 Frankfurt | NITROGEN-CONTAINING PETROLEUM EMULSION SPLITTERS AND THEIR USE |
| CN103524726B (en) * | 2013-09-26 | 2015-11-18 | 山东德仕石油工程集团股份有限公司 | The preparation method of a kind of spy, super-viscous oil emulsion splitter |
| CN103626987B (en) * | 2013-12-13 | 2015-10-21 | 山东大学 | A kind of preparation method for polymer flooding emulsion splitter |
| GB201408823D0 (en) * | 2014-05-19 | 2014-07-02 | Croda Int Plc | Demulsifiers |
-
2016
- 2016-11-29 CN CN201611068448.2A patent/CN106520184B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN106520184A (en) | 2017-03-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106520184B (en) | A kind of preparation method of high asphaltenes crude oil demulsifier | |
| CA1156953A (en) | Lime addition to heavy crude oils prior to coking | |
| CN105236798B (en) | A kind of preparation method of naphthalene water reducer | |
| DK168541B1 (en) | Use of acid-group, thermostable, hydrophilic condensation products of aldehydes and ketones | |
| CN105368423B (en) | One kind is recovered the oil and uses Chrome-free compound resin gel-like profile control agent and preparation method and purposes | |
| CA2463104A1 (en) | In situ production of a blending agent from a hydrocarbon containing formation | |
| CN107382779A (en) | One planting sand storehouse must bent intermediate preparation method | |
| CN110483577A (en) | A kind of P, N, Si ternary hybrid fire retardant and preparation method | |
| CN105693688A (en) | Reaction treatment method of heliotropin intermediate 3,4-dioxymethylene mandelic acid | |
| CN102796035A (en) | Condensation method of m-,p-mixed di-(tert-butyl isopropyl peroxide)benzene | |
| CN103028342B (en) | Sulfonate anionic/nonionic surfactant and preparation method thereof | |
| CN107267127A (en) | A kind of water shutoff agent and preparation method thereof | |
| CN106866473A (en) | A kind of high-content wax viscous crude wax is brilliant, asphaltene dispersants | |
| CN108774309A (en) | A kind of high refractive indexsulfur-containing epoxy resin and preparation method thereof | |
| CN100506827C (en) | Diphenylacetylene silane novle synthesis method | |
| CN101817782A (en) | Method for synthesizing 2-aminosulfonyl-N,N-dimethylnicotinamide | |
| CN103044272B (en) | Preparation method of 4-nitroso-N-ethyl-N-hydroxyethyl aniline | |
| CN110683968B (en) | Foaming agent for thickened oil recovery and preparation method thereof | |
| CN104744319A (en) | Production method of heavy alkyl benzene sulfonic acid for producing oil-displacing agent | |
| CN101402651A (en) | Method for preparing methyl tin thiol ester heat stabilizer | |
| CN101328174B (en) | Method for preparing 3-(2-chloroethyl)-2-methyl-4H- naphthyridine[1,2-a]pyrimidine-4-ketone | |
| CN105218577B (en) | A kind of method that use double solvents, three component catalysts synthesize γ mercaptopropyltriethoxysilanes | |
| CN105505363A (en) | Oil displacement petroleum sulfonate composition and preparation method thereof | |
| CN111825364B (en) | Preparation method of environment-friendly naphthalene water reducer | |
| CN106367053B (en) | Viscosity reduction composition and its super―heavy oil exploitation field application |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20190228 Address after: 257000 Shengli Industrial Park, Dongying District, Dongying City, Shandong Province Applicant after: SHANDONG DESHI PETROLEUM ENGINEERING GROUP CO., LTD. Applicant after: Shandong De Shi Chemical Co., Ltd. Address before: 257000 Shengli Industrial Park, Dongying District, Dongying City, Shandong Province Applicant before: SHANDONG DESHI PETROLEUM ENGINEERING GROUP CO., LTD. |
|
| TA01 | Transfer of patent application right | ||
| CB03 | Change of inventor or designer information |
Inventor after: Gao Ruimei Inventor after: Kang Xiaoyan Inventor after: Yu Changlu Inventor after: Cui Xuezhang Inventor after: Gu Zhihui Inventor after: Cui Shizhang Inventor after: Zhang Xianghong Inventor after: Wang Liming Inventor after: Han Dong Inventor after: Hou Yuexia Inventor before: Gao Ruimei Inventor before: Yu Changlu Inventor before: Gu Zhihui Inventor before: Zhang Xianghong Inventor before: Wang Liming Inventor before: Han Dong Inventor before: Hou Yuexia |
|
| CB03 | Change of inventor or designer information | ||
| CB03 | Change of inventor or designer information |
Inventor after: Gao Ruimei Inventor after: Kang Xiaoyan Inventor after: Yu Changlu Inventor after: Cui Xuezhang Inventor after: Gu Zhihui Inventor after: Cui Shizhang Inventor after: Zhang Xianghong Inventor after: Wang Liming Inventor after: Han Dong Inventor after: Hou Yuexia Inventor before: Gao Ruimei Inventor before: Kang Xiaoyan Inventor before: Yu Changlu Inventor before: Cui Xuezhang Inventor before: Gu Zhihui Inventor before: Cui Shizhang Inventor before: Zhang Xianghong Inventor before: Wang Liming Inventor before: Han Dong Inventor before: Hou Yuexia |
|
| CB03 | Change of inventor or designer information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: Building 18, youhuigu, Shengli Industrial Park, Dongying District, Dongying City, Shandong Province Co-patentee after: SHANDONG DESHI CHEMICAL Co.,Ltd. Patentee after: Deshi Energy Technology Group Co., Ltd Address before: 257000 Shengli Industrial Zone, Dongying District, Shandong, Dongying Co-patentee before: SHANDONG DESHI CHEMICAL Co.,Ltd. Patentee before: SHANDONG DESHI PETROLEUM ENGINEERING GROUP Co.,Ltd. |
|
| CP03 | Change of name, title or address | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20201124 Address after: 257000 to the north of Gangcheng Road, Dongying Port Economic Development Zone, Dongying City, Shandong Province Patentee after: SHANDONG DESHI CHEMICAL Co.,Ltd. Patentee after: Deshi Energy Technology Group Co.,Ltd. Address before: Building 18, youhuigu, Shengli Industrial Park, Dongying District, Dongying City, Shandong Province Patentee before: Deshi Energy Technology Group Co.,Ltd. Patentee before: SHANDONG DESHI CHEMICAL Co.,Ltd. |
|
| TR01 | Transfer of patent right |