CN108165302B - Preparation method of demulsifying agent for condensate oil-water emulsion - Google Patents
Preparation method of demulsifying agent for condensate oil-water emulsion Download PDFInfo
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- 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
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- 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
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- 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
- C08G65/32—Polymers modified by chemical after-treatment
- C08G65/329—Polymers modified by chemical after-treatment with organic compounds
- C08G65/331—Polymers modified by chemical after-treatment with organic compounds containing oxygen
- C08G65/332—Polymers modified by chemical after-treatment with organic compounds containing oxygen containing carboxyl groups, or halides, or esters thereof
- C08G65/3322—Polymers modified by chemical after-treatment with organic compounds containing oxygen containing carboxyl groups, or halides, or esters thereof acyclic
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- 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
- C08G8/00—Condensation polymers of aldehydes or ketones with phenols only
- C08G8/04—Condensation polymers of aldehydes or ketones with phenols only of aldehydes
- C08G8/08—Condensation polymers of aldehydes or ketones with phenols only of aldehydes of formaldehyde, e.g. of formaldehyde formed in situ
- C08G8/10—Condensation polymers of aldehydes or ketones with phenols only of aldehydes of formaldehyde, e.g. of formaldehyde formed in situ with phenol
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Abstract
The invention provides a preparation method of a demulsifying agent aiming at a condensate oil-water emulsion, wherein phenol is heated, melted and stirred, dodecylbenzene sulfonic acid and 1500# solvent oil are added, the mixture is stirred uniformly, cooled, formaldehyde is dripped, and then the mixture is heated, refluxed and split; cooling, adding potassium methoxide solution, stirring, vacuumizing the reactor, and filling nitrogen to normal pressure; dripping propylene oxide, and cooling after sampling is qualified; dropwise adding fumaric acid, blowing nitrogen after dropwise adding, heating and preserving heat; dripping p-toluenesulfonic acid, stirring, vacuumizing, controlling the temperature, stirring, continuously dripping monoethanolamine, and stirring; cooling, extracting and adding the solvent, and stirring to finish the synthesis of the product; has the advantages that: the demulsifier prepared by the invention solves the problem of stubborn emulsion on the production site of a natural gas well, and ensures that the relative recovery rate of condensate oil reaches more than 60 percent; the oil content of the sewage after the natural gas produced liquid treatment is greatly reduced, the pollution of the sewage discharge to the environment is reduced, and worries about the future development of the condensate oil gas are solved.
Description
Technical Field
The invention relates to the field of chemical treatment agents for natural gas produced liquid, in particular to a preparation method of a demulsifying agent for condensate oil-water emulsion.
Background
The exploration practice in the last ten years shows that in some oil-bearing basins of China, a plurality of natural gas reservoirs are associated with a certain amount of condensate oil (or light oil). The gas reservoir is characterized in that liquid hydrocarbon associated with natural gas is in a supercritical state under the conditions of high pressure and high temperature in a stratum, when the gas reservoir is exploited to the ground, as the pressure and the temperature are reduced, a liquid product which is condensed and separated out through reverse phase condensation is called condensate oil, the main component is a mixture of C5-C8 hydrocarbons, the condensate oil contains a small amount of hydrocarbons larger than C8 and impurities such as sulfur dioxide, thiophenes, thiols, thioether, polysulfide and the like, the fraction is mostly between 20 ℃ and 200 ℃, the gas reservoir has the advantages of small specific gravity, generally lower content of heavy hydrocarbons and non-hydrocarbon components than crude oil, good volatility and the like, and is a high-quality raw material for oil refining industry and solvent oil production.
Compared with the conventional crude oil, the condensate oil is preferred to be eaten by the oil refining device, because the condensate oil has good quality and high yield, the yield of the conventional oil in a refinery is 80 percent, and the condensate oil can reach more than 90 percent. Meanwhile, the refined product has wide application and high price. Condensate oil in China is mainly used as an oil refining raw material and an ethylene raw material, and is used for producing benzene, toluene and xylene through aromatization. As a supplementary petroleum resource, the condensate oil has the advantages of cost, processing cost, benefit and the like in the field of petrochemical industry, and is worthy of particular attention and utilization.
At present, condensate oil is also widely regarded in natural gas research. However, the development of condensate also suffers from the fact that the produced oil contains a large amount of water and forms a stable emulsion, which is very difficult to handle and forms a very tough emulsion in the form of "jellied bean curd". The gas field is usually abandoned or treated as sewage, the sewage is not up to the standard in environmental protection and safety, a large amount of energy is wasted, the productivity of a gas well is influenced, and the development of condensate oil gas energy is also restricted.
Disclosure of Invention
The invention aims to solve the defects of the prior art and provide a preparation method of a demulsifying agent for a condensate oil-water emulsion.
The new technical scheme of the invention is as follows: a preparation method of a demulsifying medicament for a condensate oil-water emulsion comprises the following preparation steps:
(1) adding phenol into a reaction kettle, heating to 90 ℃, stirring for 30 minutes after a product is melted, adding dodecylbenzene sulfonic acid, adding 1500# solvent oil, and stirring for 10 minutes. Cooling to 80 ℃, dripping formaldehyde at 75-80 ℃, and keeping the temperature for reaction for 1 hour at the temperature after dripping. Then heating, refluxing and dividing water, and controlling the temperature to be 125-155 ℃ until no water is separated out;
(2) cooling the product obtained in the step to 58-60 ℃, adding 10-20% of potassium methylate solution (mass percent of potassium methylate in methanol) from a dropwise adding tank at the upper part of a reaction kettle, uniformly stirring, vacuumizing until the pressure in the reactor reaches-0.08 MPa, and the vacuum time is more than or equal to 30 minutes until the water content is controlled below 0.05% (mass percent), stopping vacuumizing, stably heating to 135 ℃, and filling nitrogen to normal pressure; dropping propylene oxide tentatively, keeping the dropping temperature between 138 ℃ and 150 ℃ after confirming that the reaction is carried out for 30 minutes, keeping the reaction pressure below 0.2MPa, continuing dropping propylene oxide, keeping the temperature for reaction for 30 minutes after the dropping is finished, carrying out vacuum reaction for 30 minutes, and cooling to 90 ℃ after sampling and detecting are qualified;
(3) dropwise adding fumaric acid into the product synthesized in the step II at the temperature of 80-90 ℃, blowing nitrogen to 0.2MPa after dropwise adding, slowly heating to 200 ℃, and carrying out heat preservation reaction for 3 hours;
(4) cooling the product obtained in the step three to 90 ℃, slowly dripping p-toluenesulfonic acid, uniformly stirring, vacuumizing for 15 minutes, controlling the temperature to 70-90 ℃, stirring for 10 minutes after dripping is finished, continuously dripping monoethanolamine, controlling the viscosity of the product to enable the dynamic viscosity to be less than or equal to 2000mPa & s at 25 ℃, and stirring for 30 minutes while keeping the temperature;
(5) after the reaction is finished, cooling to 55 ℃, extracting the solvent, and uniformly stirring to finish the synthesis of the product.
The mass ratio of phenol to formaldehyde in the step (1) is (3-3.5): 1; the mass ratio of the dodecylbenzene sulfonic acid to the phenol is 1: 100; the mass ratio of the 1500# solvent oil to the phenol is 1: 4-1: 3.
the mass ratio of the product obtained in the step (2) to the epoxypropane is 1: (50-60). The mass ratio of the potassium methoxide solution to the propylene oxide is (1-2): 100.
The total mass of the fumaric acid in the step (3) is 1.0-2.5% of the total mass of the product synthesized in the step (II).
The total mass of the p-toluenesulfonic acid in the step (4) is 3.5-4.0% of the total mass of the product synthesized in the step (iii), and the total mass of the monoethanolamine is 1.5-4.0% of the total mass of the product synthesized in the step (iii).
Chemical reactions involved in the preparation method
The main physicochemical parameters of the demulsifier obtained by the preparation method are as follows:
the appearance is light yellow to yellow uniform liquid
RSN value: 15-16
Moisture content: less than or equal to 0.05 percent
Relative recovery rate of condensate: not less than 60 percent
Absolute dehydration rate: not less than 96%
Flash point: not less than 30 DEG C
Solidifying point: at most-10 ℃.
The invention has the beneficial effects that: the demulsifier prepared by the invention solves the problem of stubborn emulsion on the production site of a natural gas well, and realizes the separation of condensate oil and water, so that the relative recovery rate of the condensate oil reaches more than 60%; the condensate oil demulsification agent can achieve high-efficiency demulsification on natural gas produced liquid, and the interface is clear and the oil quality is clear after oil-water separation; the use of the condensate oil demulsifier greatly reduces the oil content of the sewage after the treatment of the natural gas produced liquid, reduces the pollution of the sewage discharge to the environment, also meets the safety requirement, and solves the worries of the future for further developing condensate oil gas.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
A preparation method of a demulsifying medicament for a condensate oil-water emulsion comprises the following preparation steps:
(1) adding phenol into a reaction kettle, heating to 90 ℃, stirring for 30 minutes after a product is melted, adding dodecylbenzene sulfonic acid, adding 1500# solvent oil, and stirring for 10 minutes. Cooling to 80 ℃, dripping formaldehyde at 75-80 ℃, and keeping the temperature for reaction for 1 hour at the temperature after dripping. Then heating, refluxing and dividing water, and controlling the temperature to be 125-155 ℃ until no water is separated out;
(2) cooling the product obtained in the step to 58-60 ℃, adding 10-20% of potassium methylate solution (mass percent of potassium methylate in methanol) from a dropwise adding tank at the upper part of a reaction kettle, uniformly stirring, vacuumizing until the pressure in the reactor reaches-0.08 MPa, and the vacuum time is more than or equal to 30 minutes until the water content is controlled below 0.05% (mass percent), stopping vacuumizing, stably heating to 135 ℃, and filling nitrogen to normal pressure; dropping propylene oxide tentatively, keeping the dropping temperature between 138 ℃ and 150 ℃ after confirming that the reaction is carried out for 30 minutes, keeping the reaction pressure below 0.2MPa, continuing dropping propylene oxide, keeping the temperature for reaction for 30 minutes after dropping is finished, carrying out vacuum for 30 minutes, and cooling to 90 ℃ after sampling and detecting are qualified;
(3) dropwise adding fumaric acid into the product synthesized in the step II at the temperature of 80-90 ℃, blowing nitrogen to 0.2MPa after dropwise adding, slowly heating to 200 ℃, and carrying out heat preservation reaction for 3 hours;
(4) cooling the product obtained in the step three to 90 ℃, slowly dripping p-toluenesulfonic acid, uniformly stirring, vacuumizing for 15 minutes, controlling the temperature to 70-90 ℃, stirring for 10 minutes after dripping is finished, continuously dripping monoethanolamine, controlling the viscosity of the product to enable the dynamic viscosity to be less than or equal to 2000mPa & s at 25 ℃, and stirring for 30 minutes while keeping the temperature;
(5) after the reaction is finished, cooling to 55 ℃, extracting the solvent, and uniformly stirring to finish the synthesis of the product.
The mass ratio of phenol to formaldehyde in the step (1) is (3-3.5): 1; the mass ratio of the dodecylbenzene sulfonic acid to the phenol is 1: 100; the mass ratio of the 1500# solvent oil to the phenol is 1: 4-1: 3.
the mass ratio of the product obtained in the step (2) to the epoxypropane is 1: (50-60). The mass ratio of the potassium methoxide solution to the propylene oxide is (1-2): 100.
The total mass of the fumaric acid in the step (3) is 1.0-2.5% of the total mass of the product synthesized in the step (II).
The total mass of the p-toluenesulfonic acid in the step (4) is 3.5-4.0% of the total mass of the product synthesized in the step (iii), and the total mass of the monoethanolamine is 1.5-4.0% of the total mass of the product synthesized in the step (iii).
Chemical reactions involved in the preparation method
The main physicochemical parameters of the demulsifier obtained by the preparation method are as follows:
the appearance is light yellow to yellow uniform liquid
RSN value: 15-16
Moisture content: less than or equal to 0.05 percent
Relative recovery rate of condensate: not less than 60 percent
Absolute dehydration rate: not less than 96%
Flash point: not less than 30 DEG C
Solidifying point: at most-10 ℃.
Example 1:
(1) adding 200kg of phenol into a reaction kettle, heating to 90 ℃, stirring for 30 minutes after the product is melted, adding 2kg of dodecylbenzene sulfonic acid, adding 50kg of 1500# solvent oil, and stirring for 10 minutes. Cooling to 80 ℃, dripping 66kg of formaldehyde at 75-80 ℃, and keeping the temperature for reaction for 1 hour at the temperature after dripping. Then heating, refluxing and dividing water, and controlling the temperature to be 125-155 ℃ until no water is separated out; and preparing the phenolic resin.
(2) And cooling the phenolic resin to 90 ℃, vacuumizing until the pressure in the reactor reaches-0.08 MPa, wherein the vacuum time is not less than 30 minutes, detecting the moisture until the moisture is controlled below 0.05 percent, and stopping vacuum.
(3) And cooling to 58-60 ℃, adding 160 kg of 10% potassium methoxide solution from the upper part of the reaction kettle dropwise, wherein the 10% potassium methoxide solution is the mass percent of potassium methoxide in methanol, uniformly stirring, and vacuumizing for 10 minutes again. Steadily heating to 135 ℃, charging nitrogen to normal pressure, dropping 10 Kg of propylene oxide in three trial times, reacting for 5 minutes, confirming the reaction heat release, keeping the dropping temperature between 138 ℃ and 150 ℃ after 30 minutes from the first dropping, keeping the reaction pressure below 0.2MPa, dropping 16000Kg of propylene oxide in total, keeping the temperature for 30 minutes after the dropping is finished, vacuumizing for 30 minutes, and cooling to 80 ℃ after sampling and detecting are qualified.
(4) And (3) dropwise adding 170kg of fumaric acid into the product synthesized in the step (3), blowing nitrogen to 0.2MPa after dropwise adding, and heating to 200 ℃. The reaction was incubated for 3 hours.
(5) And (3) putting 1000 kg of the demulsifier intermediate obtained in the step (4) into a reaction kettle, uniformly stirring, vacuumizing for 15 minutes, heating to 70-90 ℃, dropwise adding 40 kg of p-toluenesulfonic acid, stirring for 10 minutes after dropwise adding, continuously dropwise adding 15kg of monoethanolamine, controlling the viscosity of the product, and keeping the temperature and stirring for 30 minutes.
(6) And after the reaction is finished, cooling to 55 ℃, pumping and adding methanol, uniformly stirring, discharging and finishing the synthesis of the product.
Example 2:
(1) adding 200kg of phenol into a reaction kettle, heating to 90 ℃, stirring for 30 minutes after the product is melted, adding 2kg of dodecylbenzene sulfonic acid, adding 66kg of 1500# solvent oil, and stirring for 10 minutes. Cooling to 80 ℃, dripping 58kg of formaldehyde at 75-80 ℃, and keeping the temperature for reaction for 1 hour at the temperature after dripping. Then heating, refluxing and dividing water, and controlling the temperature to be 125-155 ℃ until no water is separated out; and preparing the phenolic resin.
(2) And cooling the phenolic resin to 90 ℃, vacuumizing until the pressure in the reactor reaches-0.08 MPa, wherein the vacuum time is not less than 30 minutes, detecting the moisture until the moisture is controlled below 0.05 percent, and stopping vacuum.
(3) And cooling to 58-60 ℃, adding 200kg of 10% potassium methoxide solution from the upper part of the reaction kettle dropwise, wherein the 10% potassium methoxide solution is the mass percent of potassium methoxide in methanol, uniformly stirring, and vacuumizing for 10 minutes again. Steadily heating to 135 ℃, charging nitrogen to normal pressure, dropping 10 Kg of butylene oxide in three trial times, reacting for 5 minutes, confirming the reaction heat release, keeping the dropping temperature between 138 ℃ and 150 ℃ after 30 minutes from the first dropping, keeping the reaction pressure below 0.2MPa, dropping 19000Kg of propylene oxide in total, keeping the temperature for 30 minutes after the dropping is finished, vacuumizing for 30 minutes, and cooling to 80 ℃ after sampling and detecting are qualified.
(4) And (3) dropwise adding 200kg of fumaric acid into the product synthesized in the step (3), blowing nitrogen to 0.2MPa after dropwise adding, and heating to 200 ℃. The reaction was incubated for 3 hours.
(5) And (3) putting 1000 kg of the demulsifier obtained in the step (4) into a reaction kettle, uniformly stirring, vacuumizing for 15 minutes, heating to 70-90 ℃, dropwise adding 35 kg of p-toluenesulfonic acid, stirring for 10 minutes after dropwise adding, continuously dropwise adding 20kg of monoethanolamine, controlling the viscosity of the product, and keeping the temperature and stirring for 30 minutes.
(6) And after the reaction is finished, cooling to 55 ℃, pumping and adding methanol, uniformly stirring, discharging and finishing the synthesis of the product.
The condensate oil water emulsion demulsification agent prepared by the method reaches the expected quality index, and is obtained from demulsification screening experiments on condensate oil in three factories, namely North China and Su Li gas fields, the product has the characteristics of small using amount, good demulsification effect, clear water after treatment, high condensate oil recovery rate and the like, and reaches the expected use standard.
Claims (2)
1. A preparation method of a demulsifying agent aiming at a condensate oil-water emulsion is characterized by comprising the following steps: the preparation steps are as follows:
(1) adding phenol into a reaction kettle, heating to 90 ℃, stirring for 30 minutes after a product is molten, and adding dodecylbenzene sulfonic acid, wherein the mass ratio of the dodecylbenzene sulfonic acid to the phenol is 1: 100; adding 1500# solvent oil, wherein the mass ratio of the 1500# solvent oil to the phenol is 1: 4-1: 3, stirring for 10 minutes, cooling to 80 ℃, and dropwise adding formaldehyde at 75-80 ℃, wherein the mass ratio of phenol to formaldehyde is (3-3.5): 1, after the dropwise addition is finished, carrying out heat preservation reaction for 1 hour at the temperature, then heating up, refluxing and dividing water, and controlling the temperature to be 125-155 ℃ until no water is separated out;
(2) cooling the product obtained in the step (1) to 58-60 ℃, adding 10-20% of potassium methylate solution (mass percent of potassium methylate in methanol) from a dropwise adding tank at the upper part of a reaction kettle, uniformly stirring, vacuumizing until the pressure in the reactor reaches-0.08 MPa, and the vacuum time is more than or equal to 30 minutes until the water content is controlled below 0.05% (mass percent), stopping vacuum, stably heating to 135 ℃, and filling nitrogen to normal pressure; dropping propylene oxide tentatively, keeping the dropping temperature between 138 ℃ and 150 ℃ after confirming that the reaction is carried out for 30 minutes, keeping the reaction pressure below 0.2MPa, continuing dropping propylene oxide, keeping the temperature for reaction for 30 minutes after the dropping is finished, carrying out vacuum reaction for 30 minutes, and cooling to 90 ℃ after sampling and detecting are qualified; the mass ratio of the product obtained in the step (1) to the propylene oxide is 1: (50-60), wherein the mass ratio of the potassium methoxide solution to the propylene oxide is (1-2) to 100;
(3) dropwise adding fumaric acid into the product synthesized in the step (2) at the temperature of 80-90 ℃, wherein the total mass of the fumaric acid is 1.0-2.5% of the total mass of the product synthesized in the step (2), blowing nitrogen to 0.2MPa after dropwise adding, slowly heating to 200 ℃, and carrying out heat preservation reaction for 3 hours;
(4) cooling the product obtained in the step (3) to 90 ℃, slowly dripping p-toluenesulfonic acid, wherein the total mass of the p-toluenesulfonic acid is 3.5-4.0% of the total mass of the product synthesized in the step (3), uniformly stirring, vacuumizing for 15 minutes, controlling the temperature to 70-90 ℃, stirring for 10 minutes after dripping, and continuously dripping monoethanolamine, wherein the total mass of the monoethanolamine is 1.5-4.0% of the total mass of the product synthesized in the step (3); controlling the viscosity of the product to ensure that the dynamic viscosity is less than or equal to 2000mPa & s at 25 ℃, and stirring for 30 minutes under heat preservation;
(5) after the reaction is finished, cooling to 55 ℃, extracting the solvent, and uniformly stirring to finish the synthesis of the product;
the preparation method comprises the following chemical reactions:
2. the method for preparing the demulsifying agent for the condensate oil-water emulsion as claimed in claim 1, wherein the demulsifying agent comprises the following components: the main physicochemical parameters of the demulsifier obtained by the preparation method are as follows:
the appearance is light yellow to yellow uniform liquid
RSN value: 15-16
Moisture content: less than or equal to 0.05 percent
Relative recovery rate of condensate: not less than 60 percent
Absolute dehydration rate: not less than 96%
Flash point: not less than 30 DEG C
Solidifying point: at most-10 ℃.
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| CN104498081A (en) * | 2015-01-09 | 2015-04-08 | 山东德仕石油工程集团股份有限公司 | Natural gas well foam draining extraction emulsion demulsifying agent |
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Address after: Building 18, youhuigu, Shengli Industrial Park, Dongying District, Dongying City, Shandong Province Applicant after: Deshi Energy Technology Group Co.,Ltd. Applicant after: SHANDONG DESHI CHEMICAL Co.,Ltd. Address before: 257000 Shengli Industrial Zone, Dongying District, Shandong, Dongying Applicant before: SHANDONG DESHI PETROLEUM ENGINEERING GROUP Co.,Ltd. Applicant before: SHANDONG DESHI CHEMICAL Co.,Ltd. |
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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. |
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