CN104498084A - Desalination and deacidification processing method for crude oil - Google Patents
Desalination and deacidification processing method for crude oil Download PDFInfo
- Publication number
- CN104498084A CN104498084A CN201410662449.4A CN201410662449A CN104498084A CN 104498084 A CN104498084 A CN 104498084A CN 201410662449 A CN201410662449 A CN 201410662449A CN 104498084 A CN104498084 A CN 104498084A
- Authority
- CN
- China
- Prior art keywords
- oil
- crude oil
- tank
- tank body
- water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
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
- C10G61/00—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen
-
- 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
- C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
-
- 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
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1033—Oil well production fluids
Abstract
The invention discloses a desalination and deacidification processing method for crude oil. The method comprises the following steps: the crude oil is unloaded to a tank, a demulsifier is added, gradual heating is carried out, the temperature is kept at 45 to 65 DEG C, dehydration is regularly carried out on the crude oil, and sampling analysis is carried out; after settling separation is completed, lighter crude oil in the upper part of the tank is diverted to a lighter crude oil tank, the demulsifier is added continuously, heating is carried out until the temperature is at 45 to 65 DEG C, and sampling analysis is carried out on the oil body in the tank; dehydration separation continues to be carried out in the lighter crude oil tank, oil body located on the upper part of mudimpurities is poured to another tank, reversed pouring and demulsifier adding are carried out for many times when poured to the another tank until the sample achieves requirements; a chemical light oilproduct achieving the requirements is diverted to a chemical light oil product tank for continuous reforming separation or directly for continuous reforming separation, and a heavy oil product achieving the requirements is diverted to a heavy oil product tank for coking processing or directly for coking processing. The desalination and deacidification processing method for crude oil has the advantages that the operation is safe, the cost is lower, processing effects are better, and better environmentally friendly performance is achieved.
Description
Technical field
The present invention relates to a kind of depickling treatment process of crude oil, the working method of especially a kind of crude oil desalting depickling.
Background technology
The most salts contg of marine oil is higher, and independent difficulty of processing is large, and oil product acid number is high, easily causes corrosion of equipment; Oil-water emulsion is serious and stable, and the bright oil of water is cut in electric desalting; After de-, crude oil desalting content is high, causes corrosion; Containing silt, very easily cause device fouling of heat exchangers and equipment corrosion aggravation; In electricity decontamination water and tank field dehydration, salts contg is higher, and sewage disposal biochemical bacteria can not tolerate, and simultaneously water contains a large amount of silt, and the greasy filth of generation not easily processes.Existing a kind of application number is that CN201210432 671.6 is called that the Chinese invention patent application of " a kind of pretreatment process of high-acid crude oil " discloses a kind of pretreatment process of high-acid crude oil, this inventive method utilizes the feature of the easy emulsification of high-acid crude oil, by water and high-acid crude oil mixing, enter aquathermolysis device and process.At relatively high temperatures, high-acid crude oil depickling cracking, simultaneous breakdown of emulsion, realizes dehydration, desalination, and effectively can solve the etching problem in treating processes this inventive method.But its shortcoming is, depickling, cracking, breakdown of emulsion manipulation require carry out in high temperature environments, and need to control air pressure, easily occur potential safety hazard, cause complex disposal process, so its technique needs to improve.
Prior art is compared, and the invention has the advantages that, tank body maintains in the envrionment temperature of 50 degrees centigrade and is separated, so operational safety, energy consumption is also low, the sampling analysis between separation period, can understand the separate stage of crude oil in time.When sampling analysis separating oil sample does not reach requirement, in comparatively light crude oil tank body, continue dehydration be separated, in the comparatively light crude oil tank body that mud foreign matter content is more, mud impurity top oil body will be arranged in and be poured into another tank body, and pour into continue to add emulsion splitter in oil body in another tank body and continue be separated, and by repeatedly pouring in down a chimney and adding emulsion splitter, until when the separating oil sample of sampling analysis reaches requirement, this treatment process, both safety also facilitated, depickling, desalination, dehydrating effect is better, and cost is also lower, and can ensure that separating oil can meet corresponding Processing Criterion before CONTINUOUS REFORMER separation or coking process, reduce percentage of admixture, improve the quality of finished product chemical industry light oil and heavy oil.From tank body or/and in oil trap, isolated sewage transport processes to sewage farm, is not separated under entering in sewage, both economizes on resources, also more environmental protection.
Summary of the invention
Technical problem to be solved by this invention provides a kind of process safety, convenience for above-mentioned prior art present situation, environmental protection and the working method of the low crude oil desalting depickling of energy consumption.
The present invention solves the problems of the technologies described above adopted technical scheme: the working method of this crude oil desalting depickling, is characterized in that: comprise the following steps,
One, unload in tank body to the crude oil containing salt, hydrogen sulfide, water and mud impurity, and add emulsion splitter, 45 ~ 65 DEG C are heated to gradually to the crude oil in tank body, keep this temperature, make moisture, mud mixes natural subsidence separation, and the crude oil between separation period regularly dewaters, sampling analysis is carried out to the crude oil between separation period, to understand the separate stage of crude oil simultaneously;
Two, by after settlement separate completing, the comparatively light crude oil on tank body top is branched to comparatively in light crude oil tank body, and continue to add emulsion splitter in comparatively light crude oil tank body, the comparatively light crude oil added in emulsion splitter is warmed to 45 ~ 65 DEG C and continues natural subsidence separation, and keep carrying out sampling analysis to understand the separation case of oil body to the oil body in tank body sepn process;
Three, comparatively plate analysis situation will be got by following principle process by light crude oil:
(1), when sampling analysis separating oil sample reaches requirement, the chemical industry light oil finished product reaching separation requirement is branched in chemical industry light oil tank body and be separated for CONTINUOUS REFORMER or be directly separated for CONTINUOUS REFORMER, the heavy oil finished product reaching separation requirement is branched to heavy oil tank for coking process or directly for coking process;
(2), if when sampling analysis separating oil sample does not reach requirement, in comparatively light crude oil tank body, continue dehydration be separated, in the comparatively light crude oil tank body that mud foreign matter content is more, mud impurity top oil body will be arranged in and be poured into another tank body, and pour into continue to add emulsion splitter in oil body in another tank body and continue be separated, and by repeatedly pouring in down a chimney and adding emulsion splitter, until when the separating oil sample of sampling analysis reaches requirement, the chemical industry light oil finished product reaching separation requirement is branched in chemical industry light oil finished product tank body and be separated for CONTINUOUS REFORMER or be directly separated for CONTINUOUS REFORMER, the heavy oil finished product reaching separation requirement is branched to heavy oil finished product tank body for coking process or directly for coking process,
Four, in step 2, after settlement separate completing, the profit of tank base and mud are diverted in oil trap, are separated further in oil trap, isolated finished product chemical industry light oil and heavy oil are delivered in corresponding tank body respectively;
Five, isolated sewage transport will process to sewage farm from tank body or/and in oil trap.
As improvement, described reformation is separated into: carry out high-temperature electric desalination to chemical industry light oil, corrected oil after high-temperature electric desalination is delivered in corresponding hold-up vessel, when after high-temperature electric desalination, the acidity of light oil does not reach requirement, light oil after electric desalting is carried out depickling process, acidity is reached requirement corrected oil and be delivered in corresponding hold-up vessel.
Improve again, the method of described high-temperature electric desalination is: insert in the tank field of 45 ~ 65 DEG C of temperature by the crude oil containing high salt, and to inject 6 ~ 8% moisture accounting for crude charging capacity concentration of reinjecting be the emulsion that the ZW2021 low-temperature demulsifying agent of 18ppm forms oil and water, emulsion being entered temperature is enter high temperature desalting and dewatering in 115 ~ 123 DEG C again, emulsion is under the strong and weak electric field of high-temperature zone and the effect of high temperature emulsion splitter, destroy the protective membrane of emulsion, water droplet is changed from small to big, continuous polymerization forms larger water droplet, because salt is water-soluble, effect by means of gravity and electric field makes salt solution settle down with separating of oil, good for upper strata crude quality is entered atmospheric and vacuum distillation unit, coker is entered by more not good enough in middle lower floor crude oil matter, brine layer is inputted sewage disposal portion, described low-temperature demulsifying agent is the ZW2021 emulsion splitter that salt tolerant is acidproof, described high temperature emulsion splitter is HZP-55 and HZP-55B emulsion splitter, described emulsion splitter is oil-soluble demulsifier or water-soluble demulsifier, and when adopting oil-soluble demulsifier, oil-soluble demulsifier injects in crude oil access to plant, and when adopting water-soluble demulsifier, water-soluble demulsifier injects before crude oil enters secondary electrical desalter mixing valve, inject the moisture of crude oil for purifying waste water or de-mineralized water, purify waste water by secondary waterflood pump injection secondary electrical desalter, inject in one-level electrical desalter by secondary electric desalting waterflood pump again, inject one-level electric desalting injection point and have two: one before interchanger, one before crude oil enters one-level electrical desalter mixing tank, first when after can making desalination by adjusting mixer, saliferous reaches process chart index request, then water note is before one-level electric desalting mixing tank, when mixing valve reaches 100%, when after desalination, saliferous still exceedes process chart requirement, then water is noted before interchanger, the degree of mixing between profit is increased by interchanger, from tank body or/and in oil trap, first isolated sewage send the Water Tank in first set sewage farm and ballast tank deposit separately and carry out settlement separate, isolated corrected oil is delivered to corrected oil to store in tank body, and the sewage transport separated second is overlapped in sewage farm and is entered environmental protection treatment to sewage, good for upper strata crude quality is entered atmospheric and vacuum distillation unit, is separated for CONTINUOUS REFORMER or is directly separated for CONTINUOUS REFORMER, coker is entered, for coking process or directly for coking process by more not good enough in middle lower floor crude oil matter.
Improve again, described de-acid-treated method is: the light oil that acidity is not up to standard after electric desalting adds de-acidying agent, de-acidying agent stoste and water mix rear injection deacidification system in 1: 7 ratio, special storage tank delivered to by settlement separate rear product oil outside transferpump, the emulsion that deacidification produces is by delivering to appointment storage tank outside depickling recycle pump, and described de-acidying agent is capacitive oil de-acidying agent.
Improve, described de-acidying agent adopts Jinan three smelting F5 type capacitive oil de-acidying agent again.
Improving, is the 15th day of a month 15th day of a month to 2 by the settlement separate time being heated to Crude Oil gradually in step one again.
Improve, the settlement separate temperature of crude oil is 50 DEG C again.
Improve again, by add in step 2 in emulsion splitter compared with light crude oil be warmed to 45 ~ 65 DEG C continue natural subsidence be separated times be 2.5 to 3.5 days.
Improve, the comparatively light crude oil added in emulsion splitter is warmed to 50 DEG C and continues natural subsidence separation again, and settlement separate 3 days.
Improve again, from tank body or/and in oil trap isolated sewage first first set be delivered to Water Tank in sewage farm and ballast tank is deposited separately and carries out settlement separate, isolated corrected oil is delivered to corrected oil to store in tank body, and the sewage transport separated second is overlapped in sewage farm and is entered environmental protection treatment to sewage.
Embodiment
Below in conjunction with embodiment, the present invention is described in further detail.
The working method of the crude oil desalting depickling of the present embodiment, comprises the following steps, and the working method of this crude oil desalting depickling, is characterized in that: comprise the following steps,
One, unload in tank body to the crude oil containing salt, hydrogen sulfide, water and mud impurity, and add emulsion splitter, 45 ~ 65 DEG C are heated to gradually to the crude oil in tank body, keep this temperature, make moisture, mud mixes natural subsidence separation, and the crude oil between separation period regularly dewaters, sampling analysis is carried out to the crude oil between separation period, to understand the separate stage of crude oil simultaneously;
Two, by after settlement separate completing, the comparatively light crude oil on tank body top is branched to comparatively in light crude oil tank body, and continue to add emulsion splitter in comparatively light crude oil tank body, the comparatively light crude oil added in emulsion splitter is warmed to 45 ~ 65 DEG C and continues natural subsidence separation, and keep carrying out sampling analysis to understand the separation case of oil body to the oil body in tank body sepn process;
Three, comparatively plate analysis situation will be got by following principle process by light crude oil:
(1), when sampling analysis separating oil sample reaches requirement, the chemical industry light oil finished product reaching separation requirement is branched in chemical industry light oil tank body and be separated for CONTINUOUS REFORMER or be directly separated for CONTINUOUS REFORMER, the heavy oil finished product reaching separation requirement is branched to heavy oil tank for coking process or directly for coking process;
(2), if when sampling analysis separating oil sample does not reach requirement, in comparatively light crude oil tank body, continue dehydration be separated, in the comparatively light crude oil tank body that mud foreign matter content is more, mud impurity top oil body will be arranged in and be poured into another tank body, and pour into continue to add emulsion splitter in oil body in another tank body and continue be separated, and by repeatedly pouring in down a chimney and adding emulsion splitter, until when the separating oil sample of sampling analysis reaches requirement, the chemical industry light oil finished product reaching separation requirement is branched in chemical industry light oil finished product tank body and be separated for CONTINUOUS REFORMER or be directly separated for CONTINUOUS REFORMER, the heavy oil finished product reaching separation requirement is branched to heavy oil finished product tank body for coking process or directly for coking process,
Four, in step 2, after settlement separate completing, the profit of tank base and mud are diverted in oil trap, are separated further in oil trap, isolated finished product chemical industry light oil and heavy oil are delivered in corresponding tank body respectively;
Five, isolated sewage transport will process to sewage farm from tank body or/and in oil trap.
Described reformation is separated into: carry out high-temperature electric desalination to chemical industry light oil, corrected oil after high-temperature electric desalination is delivered in corresponding hold-up vessel, when after high-temperature electric desalination, the acidity of light oil does not reach requirement, light oil after electric desalting is carried out depickling process, acidity is reached requirement corrected oil and be delivered in corresponding hold-up vessel.The method of described high-temperature electric desalination is: insert in the tank field of 45 ~ 65 DEG C of temperature by the crude oil containing high salt, and to inject 6 ~ 8% moisture accounting for crude charging capacity concentration of reinjecting be the emulsion that the ZW2021 low-temperature demulsifying agent of 18ppm forms oil and water, emulsion being entered temperature is enter high temperature desalting and dewatering in 115 ~ 123 DEG C again, emulsion is under the strong and weak electric field of high-temperature zone and the effect of high temperature emulsion splitter, destroy the protective membrane of emulsion, water droplet is changed from small to big, continuous polymerization forms larger water droplet, because salt is water-soluble, effect by means of gravity and electric field makes salt solution settle down with separating of oil, good for upper strata crude quality is entered atmospheric and vacuum distillation unit, coker is entered by more not good enough in middle lower floor crude oil matter, brine layer is inputted sewage disposal portion, described low-temperature demulsifying agent is the ZW2021 emulsion splitter that salt tolerant is acidproof, described high temperature emulsion splitter is HZP-55 and HZP-55B emulsion splitter.Described de-acid-treated method is: the light oil that acidity is not up to standard after electric desalting adds de-acidying agent, de-acidying agent stoste and water mix rear injection deacidification system in 1: 7 ratio, special storage tank delivered to by settlement separate rear product oil outside transferpump, the emulsion that deacidification produces is by delivering to appointment storage tank outside depickling recycle pump, and described de-acidying agent is capacitive oil de-acidying agent.Described de-acidying agent adopts Jinan three smelting F5 type capacitive oil de-acidying agent.It is the 15th day of a month 15th day of a month to 2 by the settlement separate time being heated to Crude Oil gradually in step one.The settlement separate temperature of crude oil is 50 DEG C.By add in step 2 in emulsion splitter compared with light crude oil be warmed to 45 ~ 65 DEG C continue natural subsidence be separated times be 2.5 to 3.5 days.The comparatively light crude oil added in emulsion splitter is warmed to 50 DEG C and continues natural subsidence separation, and settlement separate 3 days.From tank body or/and in oil trap isolated sewage first first set be delivered to Water Tank in sewage farm and ballast tank is deposited separately and carries out settlement separate, isolated corrected oil is delivered to corrected oil to store in tank body, and the sewage transport separated second is overlapped in sewage farm and is entered environmental protection treatment to sewage.
Precaution:
One, tank is divided in harbour emptying, tank field:
After crude oil carrier alongside, considering that aging stream spends former Water in oil, silt content large, there is quality discrepancy with top, cabin oil product in bilge oil, understands boats and ships cargo tank Nei Shui, mud deposition conditions by means such as sampling, meterings, the agreed program of unloading a ship of last and ship.During emptying, the bilge oil of inferior quality unloads to V152A tank, receives after oil about 10000 tons, change and unload to V152B tank (water content is high, sediment contamination amount is large) until V152A tank.
Two, intensification, injecting:
After crude oil enters tank, maintain that this is temperature-resistant after crude oil temperature in tank is heated to 50 DEG C gradually (temperature must not higher than 70 DEG C), heat-processed does not make crude oil form thermal convection as far as possible, makes that moisture, mud are assorted can natural subsidence be separated.Regularly petroleum tank is dewatered during heat temperature raising.Estimate about 2 months settlement separate time, sampling analysis can be carried out to upper lower floor crude oil during this period, understand separation case in time.
After profit is settlement separate, the oil trap that bottom profit (mud) incision is preset is separated, and in tank (the supposing V152A) tank of mixing few by moisture, mud, middle and upper part crude oil pours V153C tank (turning in advance) into by crude oil pump.According to dehydration, desliming situation, continue to add emulsion splitter in tank switching process.Sedimentation, after 3 days, carries out sampling analysis to V153C pot bottom, according to sampling analysis situation by following principle process:
(1) as sample reaches processing request, chemical industry light oil is treated for CONTINUOUS REFORMER, and heavy oil is treated for coking;
(2) if sampling analysis effect is poor, then pour the crude oil of less than 0.5 meter in V153C tank into moisture, mud mixes in the many tank V-152B tank of content, after the clear tank of V152A tank terminates, V153C surplus oil is poured in V-152A tank and continue to be separated, continue to add emulsion splitter in tank switching process, by repeatedly pouring in down a chimney, injecting is until meet Eligibility requirements.
Three, sewage disposal:
The sewage be separated is delivered to the Water Tank in a set of sewage farm through transferpump through Water Sproading pipeline and ballast tank is deposited separately, and buffer memory is settlement separate.Then enter two cover sewage farms and progressively regulate process.
Major objective of the present invention:
For stream flower crude oil height saliferous characteristic one, carry out the technical study of " four de-bacterium " of desalination, deodorization, depickling, de-oiling and Facultative Halophiles, form the Technology of processing stream flower crude oil, improve the working ability of crude oil with poor quality.
Main completing technology index:
(1) the pretreated poor quality stream in tank field flower crude oil reaches saliferous≤50mgNacl/l, moisture≤0.3%.Qualification rate is more than 90%.
(2) electric desalting reaches saliferous≤5mgNacl/l, oil-containing≤200mg/l in electric decontamination water after taking off, moisture after de-≤0.3%, qualification rate more than 90%.
(3) develop deacidifying process, depickling process is carried out, acid removal rate >=30% to straight run industrial fuel oil.
(4) process of Daxie petrochemical industry height saline sewage separately set up the project order tackling key problem.When reaching COD < 50mg/L after the petrifaction sewage process of Zhoushan, ammonia nitrogen < 5mg/L, reclamation rate reaches more than 50%.
Main research of the present invention:
(1) for stream flower crude oil height saliferous characteristic, the research of technology of electric de-salting and emulsion splitter is carried out.
(2) for the rich hydrogen sulfide characteristic of stream flower crude oil, deodorizing technology research is carried out.
(3) higher for stream flower acid value for crude oil, exploitation straight-run fuel oil depickling treatment process.
(4) for the high salt sewage produced in stream flower crude refining process, the research of exploitation de-oiling technique and salt tolerant biochemical bacteria.
Gordian technique of the present invention (comprising technological difficulties, innovative point):
(1) technological difficulties
The high salt flowage that contains is spent crude water emulsification serious and stablizes, and containing silt, very easily cause electric desalting to cut the bright oil of water, breakdown of emulsion degree is not high, and desalination, dehydration all not easily realize, and take off rear sewage with oil, salt is higher, intractability is large.Improve ratio of desalinization, reducing oil-containing in water, improve biochemical bacteria salt resistance ability, is the technological difficulties of this project.
(2) innovative point
One is the Research on processing technology success of the rich hydrogen sulfide crude oil of high saliferous, changes the high saliferous crude oil with poor quality of processing and depends merely on the present situation of mixing refining, effectively widen Crude oil from CNOOC processing route.
Two is cultivate the biochemical bacterial classification of strengthening salt tolerant, improves high saline sewage processing power, increases reusing sewage rate.
The value of the technology of the present invention exploitation:
(1) a high saliferous rich hydrogen sulfide stream flower crude oil complete processing is studied.
The most salts contg of marine oil is higher, and independent difficulty of processing is large, and oil product acid number is high, easily causes corrosion of equipment; Oil-water emulsion is serious and stable, and the bright oil of water is cut in electric desalting; After de-, crude oil desalting content is high, causes corrosion; Containing silt, very easily cause device fouling of heat exchangers and equipment corrosion aggravation; In electricity decontamination water and tank field dehydration, salts contg is higher, and sewage disposal biochemical bacteria can not tolerate, and simultaneously water contains a large amount of silt, and the greasy filth of generation not easily processes.Current Hai You subordinate refinery also none family can process separately for high-salt crude oil.Convection current flower crude oil complete processing is carried out technical study and is formed stream flower crude oil complete processing guiding opinion, forms high-salt crude oil machining process route, has good demonstration meaning to the processing of high saliferous ocean.
(2) be the realization of Hai You main office 5,000 ten thousand tons of oil and gas production goal tasks, realize sea oil " marine grand celebration " construction, for " secondary leap " contributes.
The feasibility of key of development technology and venture analysis:
Realize reaching electric desalting de-after reach saliferous≤5mgNacl/l, oil-containing≤200mg/l in electric decontamination water, the target of moisture after de-≤0.3%, key be de-before salt content in crud oil≤50mgNacl/l, moisture≤0.3%, therefore the crude oil tank farm pre-treatment of stream flower is most important.According to experience and the domestic and international low-temperature demulsifying agent production development of Daxie, Ningbo in 2010/Zhoushan petrochemical industry treatment of aged stream caul-fat, tank field pretreatment goal is feasible.Zhoushan petrifaction sewage process proceeds to certain phase by the screening of salt tolerant high-efficiency strain, now can realize near zero release.Oil removing ability and sewage farm transformation is improved by increasing upper equipment, carry out biological reinforced, improve biochemical bacteria tolerance, when reaching COD < 50mg/L after sewage disposal, ammonia nitrogen < 5mg/L, it is feasible that reclamation rate reaches more than 50% target.This invention production risk is less, contributes to extra large oily secondary and crosses over planning, meet the planning of national Long-and Medium-term Development.
The present invention can also carry out de-oiling to sewage, add that in tank, tank de-oiling technology carries out oil removing by air-float technology oil removing, the present invention passes through biological reinforcing technology to sewage disposal, BZT is adopted to denitrogenate-nitrated bacterial classification successful, Zhoushan petrochemical industry has 40t/h sewage stripping device and 50m3/h sewage farm, is made up of sewage degrease (coagulation), biochemical (second-stage treatment), sewage reasonable sanding and mud (scum silica frost) appropriate enrichment facility.Stream flower crude oil institute decontamination water, because saliferous is high, oil-contg is high, impacts larger to biochemical bacteria.For stream caul-fat electricity decontamination water height oil-containing, high saliferous, difficult biochemical feature, study by increasing upper equipment and sewage farm transformation, select the air-float technology oil removing matched with A/O technique, and the biochemical bacterial classification of Selection of Salt-Tolerant, adopt biological reinforcing technology, use BZT to denitrogenate-nitrated bacterial classification high-efficiency strain biofilm soft-filler, carry out biological reinforced, improve biochemical bacteria tolerance, improve oil removing ability.
Claims (9)
1. a working method for crude oil desalting depickling, is characterized in that: comprise the following steps,
One, unload in tank body to the crude oil containing salt, hydrogen sulfide, water and mud impurity, and add emulsion splitter, 45 ~ 65 DEG C are heated to gradually to the crude oil in tank body, keep this temperature, make moisture, mud mixes natural subsidence separation, and the crude oil between separation period regularly dewaters, sampling analysis is carried out to the crude oil between separation period, to understand the separate stage of crude oil simultaneously;
Two, by after settlement separate completing, the comparatively light crude oil on tank body top is branched to comparatively in light crude oil tank body, and continue to add emulsion splitter in comparatively light crude oil tank body, the comparatively light crude oil added in emulsion splitter is warmed to 45 ~ 65 DEG C and continues natural subsidence separation, and keep carrying out sampling analysis to understand the separation case of oil body to the oil body in tank body sepn process;
Three, comparatively plate analysis situation will be got by following principle process by light crude oil:
(1), when sampling analysis separating oil sample reaches requirement, the chemical industry light oil finished product reaching separation requirement is branched in chemical industry light oil tank body and be separated for CONTINUOUS REFORMER or be directly separated for CONTINUOUS REFORMER, the heavy oil finished product reaching separation requirement is branched to heavy oil tank for coking process or directly for coking process;
(2), if when sampling analysis separating oil sample does not reach requirement, in comparatively light crude oil tank body, continue dehydration be separated, in the comparatively light crude oil tank body that mud foreign matter content is more, mud impurity top oil body will be arranged in and be poured into another tank body, and pour into continue to add emulsion splitter in oil body in another tank body and continue be separated, and by repeatedly pouring in down a chimney and adding emulsion splitter, until when the separating oil sample of sampling analysis reaches requirement, the chemical industry light oil finished product reaching separation requirement is branched in chemical industry light oil finished product tank body and be separated for CONTINUOUS REFORMER or be directly separated for CONTINUOUS REFORMER, the heavy oil finished product reaching separation requirement is branched to heavy oil finished product tank body for coking process or directly for coking process,
Four, in step 2, after settlement separate completing, the profit of tank base and mud are diverted in oil trap, are separated further in oil trap, isolated finished product chemical industry light oil and heavy oil are delivered in corresponding tank body respectively;
Five, isolated sewage transport will process to sewage farm from tank body or/and in oil trap.
2. working method according to claim 1, it is characterized in that: described reformation is separated into: high-temperature electric desalination is carried out to chemical industry light oil, corrected oil after high-temperature electric desalination is delivered in corresponding hold-up vessel, when after high-temperature electric desalination, the acidity of light oil does not reach requirement, light oil after electric desalting is carried out depickling process, acidity is reached requirement corrected oil and be delivered in corresponding hold-up vessel.
3. working method according to claim 2, it is characterized in that: the method for described high-temperature electric desalination is: the crude oil containing high salt is inserted in the tank field of 45 ~ 65 DEG C of temperature, and to inject 6 ~ 8% moisture accounting for crude charging capacity concentration of reinjecting be the emulsion that the ZW2021 low-temperature demulsifying agent of 18ppm forms oil and water, emulsion being entered temperature is enter high temperature desalting and dewatering in 115 ~ 123 DEG C again, emulsion is under the strong and weak electric field of high-temperature zone and the effect of high temperature emulsion splitter, destroy the protective membrane of emulsion, water droplet is changed from small to big, continuous polymerization forms larger water droplet, because salt is water-soluble, effect by means of gravity and electric field makes salt solution settle down with separating of oil, good for upper strata crude quality is entered atmospheric and vacuum distillation unit, coker is entered by more not good enough in middle lower floor crude oil matter, brine layer is inputted sewage disposal portion, described low-temperature demulsifying agent is the ZW2021 emulsion splitter that salt tolerant is acidproof, described high temperature emulsion splitter is HZP-55 and HZP-55B emulsion splitter, described emulsion splitter is oil-soluble demulsifier or water-soluble demulsifier, and when adopting oil-soluble demulsifier, oil-soluble demulsifier injects in crude oil access to plant, and when adopting water-soluble demulsifier, water-soluble demulsifier injects before crude oil enters secondary electrical desalter mixing valve, inject the moisture of crude oil for purifying waste water or de-mineralized water, purify waste water by secondary waterflood pump injection secondary electrical desalter, inject in one-level electrical desalter by secondary electric desalting waterflood pump again, inject one-level electric desalting injection point and have two: one before interchanger, one before crude oil enters one-level electrical desalter mixing tank, first when after can making desalination by adjusting mixer, saliferous reaches process chart index request, then water note is before one-level electric desalting mixing tank, when mixing valve reaches 100%, when after desalination, saliferous still exceedes process chart requirement, then water is noted before interchanger, the degree of mixing between profit is increased by interchanger, from tank body or/and in oil trap, first isolated sewage send the Water Tank in first set sewage farm and ballast tank deposit separately and carry out settlement separate, isolated corrected oil is delivered to corrected oil to store in tank body, and the sewage transport separated second is overlapped in sewage farm and is entered environmental protection treatment to sewage, good for upper strata crude quality is entered atmospheric and vacuum distillation unit, is separated for CONTINUOUS REFORMER or is directly separated for CONTINUOUS REFORMER, coker is entered, for coking process or directly for coking process by more not good enough in middle lower floor crude oil matter.
4. working method according to claim 2, it is characterized in that: described de-acid-treated method is: the light oil that acidity is not up to standard after electric desalting adds de-acidying agent, de-acidying agent stoste and water mix rear injection deacidification system in 1: 7 ratio, special storage tank delivered to by settlement separate rear product oil outside transferpump, the emulsion that deacidification produces is by delivering to appointment storage tank outside depickling recycle pump, and described de-acidying agent is capacitive oil de-acidying agent.
5. working method according to claim 4, is characterized in that: described de-acidying agent adopts Jinan three smelting F5 type capacitive oil de-acidying agent.
6. working method according to claim 5, is characterized in that: the settlement separate temperature of crude oil is 50 DEG C.
7. according to described working method arbitrary in claim 1 to 6, it is characterized in that: being warmed to 45 ~ 65 DEG C compared with light crude oil to continue the times that natural subsidence are separated be 2.5 to 3.5 days in emulsion splitter will be added in step 2.
8. working method according to claim 7, is characterized in that: the comparatively light crude oil added in emulsion splitter is warmed to 50 DEG C and continues natural subsidence separation, and settlement separate 3 days.
9. according to described working method arbitrary in claim 1 to 5, it is characterized in that: from tank body or/and in oil trap isolated sewage first first set be delivered to Water Tank in sewage farm and ballast tank is deposited separately and carries out settlement separate, isolated corrected oil is delivered to corrected oil to store in tank body, and the sewage transport separated second is overlapped in sewage farm and is entered environmental protection treatment to sewage.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410662449.4A CN104498084B (en) | 2014-11-15 | 2014-11-15 | The processing method of crude oil desalting depickling |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410662449.4A CN104498084B (en) | 2014-11-15 | 2014-11-15 | The processing method of crude oil desalting depickling |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104498084A true CN104498084A (en) | 2015-04-08 |
| CN104498084B CN104498084B (en) | 2017-06-27 |
Family
ID=52939542
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410662449.4A Expired - Fee Related CN104498084B (en) | 2014-11-15 | 2014-11-15 | The processing method of crude oil desalting depickling |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104498084B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104974775A (en) * | 2015-05-22 | 2015-10-14 | 中石寰球（北京）工程管理咨询有限公司 | Desalination purification method for coal tar |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3658695A (en) * | 1970-12-14 | 1972-04-25 | Phillips Petroleum Co | Production of low-metal content gas oil from topped crude oil |
| CN102757813A (en) * | 2012-07-24 | 2012-10-31 | 华东理工大学 | Crude oil processing unit containing electro-desalted sewage oil remover and method of crude oil processing unit |
| CN104046380A (en) * | 2013-03-15 | 2014-09-17 | 中石化洛阳工程有限公司 | Inferior crude oil pretreatment technology |
-
2014
- 2014-11-15 CN CN201410662449.4A patent/CN104498084B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3658695A (en) * | 1970-12-14 | 1972-04-25 | Phillips Petroleum Co | Production of low-metal content gas oil from topped crude oil |
| CN102757813A (en) * | 2012-07-24 | 2012-10-31 | 华东理工大学 | Crude oil processing unit containing electro-desalted sewage oil remover and method of crude oil processing unit |
| CN104046380A (en) * | 2013-03-15 | 2014-09-17 | 中石化洛阳工程有限公司 | Inferior crude oil pretreatment technology |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104974775A (en) * | 2015-05-22 | 2015-10-14 | 中石寰球（北京）工程管理咨询有限公司 | Desalination purification method for coal tar |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104498084B (en) | 2017-06-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US9926497B2 (en) | Method to remove metals from petroleum | |
| CN103805227B (en) | A kind of pretreatment process method of high-acid crude oil | |
| US8980080B2 (en) | System and process for integrated oxidative desulfurization, desalting and deasphalting of hydrocarbon feedstocks | |
| SA517380760B1 (en) | Integrated Process to Produce Asphalt, Petroleum Green Coke, and Liquid and Gas Coking Unit Products | |
| RU2006134619A (en) | USE OF GAS FROM THE DEPOSIT FOR PRELIMINARY PROCESSING OF NATURAL RAW OIL TO PRELIMINARY CLEANING CONTAINING ASPHALTES RAW MATERIAL FOR OIL PROCESSING PA AND LIQUID RESIDUAL RAW FOR OIL | |
| Lin et al. | Progress in the technology for desulfurization of crude oil | |
| CN108203592A (en) | A kind of Desalting and Dewatering from Crude Oil equipment and its application | |
| WO2014003943A1 (en) | Decontamination of deoxygenated biomass-derived pyrolysis oil using ionic liquids | |
| CN102491578B (en) | Method for stripping emptying tower top sewage by utilizing coke tower waste heat | |
| CN105713658A (en) | Low-temperature coal tar pretreatment technology | |
| CN104498084A (en) | Desalination and deacidification processing method for crude oil | |
| RU2462501C1 (en) | Method of demetallisation and crude oil desulfurisation in flow | |
| CN203187636U (en) | Desalting and dehydration pre-treatment device of inferior-quality crude oil | |
| CN103102932B (en) | Hydrocarbon modification separation method | |
| CN110407423B (en) | Resource recovery processing device for oily sludge | |
| CN110104704B (en) | Method and device for treating dirty oil by sulfur-containing sewage | |
| CN105950212A (en) | Aged sump oil treatment process | |
| CN110104729A (en) | A kind of method and device of tank skin heating type sump oil sedimentation | |
| CN102807891B (en) | System and method for processing condensate oil | |
| CN104830514B (en) | A kind of renovation process of waste lubricating oil | |
| Li et al. | Studies on Fushun shale oil furfural refining | |
| CN104046380B (en) | A kind of crude oil with poor quality pretreatment technology | |
| CN108219834B (en) | Crude oil quality-grading treatment method | |
| WO2016028192A1 (en) | Raw hydrocarbon refining plant for northern regions | |
| KR101718965B1 (en) | A method for treating heavy crude oil using liquefied hydrocarbon oil and an apparatus for treating heavy crude oil using thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20170627 Termination date: 20211115 |