CN105273759B - A kind of method and its design method and purposes for removing crystal salt - Google Patents
A kind of method and its design method and purposes for removing crystal salt Download PDFInfo
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- CN105273759B CN105273759B CN201510696047.0A CN201510696047A CN105273759B CN 105273759 B CN105273759 B CN 105273759B CN 201510696047 A CN201510696047 A CN 201510696047A CN 105273759 B CN105273759 B CN 105273759B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B08—CLEANING
- B08B—CLEANING IN GENERAL; PREVENTION OF FOULING IN GENERAL
- B08B9/00—Cleaning hollow articles by methods or apparatus specially adapted thereto
- B08B9/02—Cleaning pipes or tubes or systems of pipes or tubes
- B08B9/027—Cleaning the internal surfaces; Removal of blockages
-
- 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
- C10G75/00—Inhibiting corrosion or fouling in apparatus for treatment or conversion of hydrocarbon oils, in general
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F16—ENGINEERING ELEMENTS AND UNITS; GENERAL MEASURES FOR PRODUCING AND MAINTAINING EFFECTIVE FUNCTIONING OF MACHINES OR INSTALLATIONS; THERMAL INSULATION IN GENERAL
- F16L—PIPES; JOINTS OR FITTINGS FOR PIPES; SUPPORTS FOR PIPES, CABLES OR PROTECTIVE TUBING; MEANS FOR THERMAL INSULATION IN GENERAL
- F16L58/00—Protection of pipes or pipe fittings against corrosion or incrustation
Abstract
The method and its design method and purposes of a kind of removing crystal salt of the present invention, the removal methods set at least one concentration detector in the wastewater outlet pipeline of afterbody separator, detect the concentration of tamper in the waste water converged after the location of water injection water filling is rinsed, and determine to block the species of material, then it is 50 1000 times of each tamper saturated concentration water requirement to control the water injection rate of each location of water injection according to tamper concentration and species, the pipeline between pipeline and/or separator and/or separator of the location of water injection between reactor and separator.The removal methods are applied to equipment and pipeline in slurry bed system hydrogenation technique, solve the problems, such as that the amount of the accessory substance such as crystalline material in hydrogenation products is big, monitor tamper content in real time, fall tamper in removing hydrogenation plant and pipeline in time, reduce the nitrogen in hydrogenation products and in separated fluid oil intermediate product, content of beary metal.
Description
Technical field
The present invention relates to a kind of method and its design method and purposes for removing crystal salt in hydrogenation plant and pipeline, at the same time
The tamper such as metal salt and other accessory substances can be also removed, belongs to petrochemical industry and coal chemical technology.
Background technology
Mink cell focus (including residual oil, catalytic slurry, de-oiled asphalt and coal tar) slurry bed system hydrogen addition technology, oily coal mix in recent years
Refining and the research of direct coal liquefaction technology (core process is slurry bed hydroprocessing) are in the ascendant, and main cause is slurry bed hydroprocessing
Technique can efficiently use heavy oil resources and coal resources, remove the impurity such as sulphur, nitrogen and heavy metal in raw material, improve at the same time
The yield and quality of light oil, and then improve the economic benefit of processing enterprise.However, since reaction mass can give birth in hydrogenation reaction
Into the crystal salts such as ammonium hydrogen carbonate, ammonium sulfide, metal salt and other accessory substances, these salt can crystallize precipitation, and its in low temperature
Its accessory substance deposits to together blocks pipeline, wear equipment and pump valve on tube wall, cause the adverse consequences such as shut-down.Add compared to conventional
Hydrogen production device, heavy-oil slurry hydrogenation, the sulfur-bearing of DCL/Direct coal liquefaction and raw material handled by oily coal calendering process, nitrogen, amount of metal and its
Its impurity is often the amount bigger of the accessory substance such as higher, the crystalline material generated after hydrogenation reaction, if these materials are not in time
Removing is fallen, and causes blocking and abrasion to hydrogenation plant and pipeline, or even causes equipment to stop maintenance, seriously affects whole factory
Manufacturing schedule, increase production cost.
At present, it is typically using the method in conventional hydro reaction, i.e., using desalted water to this way to solve the problem
Rinse block pipeline removing crystal salt, desalted water refer to remove soft water in hydroxide ion, sodium ion, sulfate ion and make
Into a kind of water quality, soft water refers to remove the calcium and magnesium ion in fresh water and the water quality that is formed.Filling pipe is generally located at position
Between the heat exchanger before high-pressure separator and air-cooled phase, and a filling pipe, high-pressure separator one are usually only set
As be 1~2.Backwashing manner includes continuous or irregularly arbitrarily rinses two ways, and wherein continuous flushing mode is to blocking
Pipeline discharges water flushing always, the advantage of doing so is that flushing effect is preferable, but desalted water continual rinsing, serious waste water resource.
Irregularly arbitrarily backwashing manner be when finding to contain more ammonium salt or metal ion in liquid oil product or discovering device or
When pipeline blocks, just discharge water and be rinsed, although water resource can be saved effectively, to the blocking in the pipeline that has blocked
Thing is rinsed and is not thorough, and especially to slightly soluble and material not soluble in water, equipment and pipe wear and blocking is caused, so oil plant
Can often replace reactor after heat exchanger and air cooler heat exchanger tube.In addition, even if it is also what is mended the fold after the sheep is lost to be rinsed
Way, intermediate products before enter next process and can not remedy containing impurity such as crystal salt and metal salts, and
And an injection point is very little, removing crystal salt is caused to be not thorough.Therefore, the prior art is to crystal salt in hydrogenation plant and pipeline
Processing mode is not planned reasonably, can not meet requirement of the slurry bed system hydrogenation reaction to removing tamper.
The content of the invention
Based on problems of the prior art, the present invention provides a kind of hydrogenation plant and crystal salt in pipeline of removing
Method, selects suitable injection point to set filling pipe, and determines water injection rate according to the solubility of crystalline material in water, ensures
Its concentration is far below saturated concentration.Effectively contained crystal in reactor outlet oil and other materials that may be blocked are separated
Out, wastewater treatment equipment is sent to.
Technical scheme：
A kind of method for removing crystal salt in hydrogenation plant and pipeline, it is characterised in that at least in afterbody separator
Concentration detector is set in wastewater outlet pipeline, detects the concentration of crystal salt in the waste water converged after location of water injection water filling is rinsed,
Then the water injection rate of location of water injection control as 50-1500 times of crystal salt saturated concentration water requirement according to crystallization salinity, it is described
Pipeline between pipeline and/or separator and/or separator of the location of water injection between reactor and separator.
The preferable separator include multiple high-pressure separators that light fraction outlet is contacted successively, temperature reduces successively and
Multiple normal pressure separators that light fraction outlet corresponding with high-pressure separator is contacted successively, the restructuring of each high-pressure separator
The light fraction outlet of the sub-export normal pressure separator identical with corresponding temperature communicates.
The high-temperature high-pressure separator, medium temperature high-pressure separator, room temperature that further preferred separator includes contacting successively are high
Press separator, and low-voltage high-temperature separator, low pressure medium temperature separator and the low pressure normal temperature separator contacted successively, location of water injection
The pipeline between pipeline, each high-pressure separator before respectively described high-temperature high-pressure separator entrance, it is described last
Primary separator is normal temperature and pressure separator.
Valve and sensor are preferably set on the filling pipe, and the sensor connects with the concentration detector
Connect.
The valve is preferably internally piloted valve and/or hand valve.
Preferably there is 1-8 water injecting pipeline in each location of water injection.
The injection water quality is preferably desalted water.
Preferable water filling temperature is 15-200 DEG C, pressure 1.0-25.0MPa.
The purposes of the method for crystal salt in above-mentioned removing hydrogenation plant and pipeline, it is characterised in that for heavy-oil hydrogenation work
The reactor and separator of skill, direct coal liquefaction process and oily coal calendering process, the heavy oil hydrogenation process refer to residual oil, catalysis
Slurry oil, de-oiled asphalt, the one or more of coal tar are combined as raw material and are processed；The oil coal calendering process refers to original
One or more kinds of combinations in oil, residual oil, catalytic slurry, de-oiled asphalt and coal tar and one kind in lignite, bituminous coal or
Multiple combinations are processed for raw material, and the proportion of oil and coal is 97-30:3-70.
A kind of design method for removing crystal salt in hydrogenation plant and pipeline, it is characterised in that design is at least in afterbody
Concentration detector is set in the wastewater outlet pipeline of separator, detects crystal salt in the waste water converged after location of water injection water filling is rinsed
Concentration, the water injection rate of each location of water injection is then controlled as each tamper saturated concentration water requirement according to tamper concentration
50-1500 times, between pipeline and/or separator and/or separator of the location of water injection between reactor and separator
Pipeline.
The technique effect of the present invention：
The method of crystal salt, goes out in the waste water of afterbody separator in a kind of the removing hydrogenation plant and pipeline of the present invention
Concentration detector is set on mouth pipeline, the waste strength of its discharge is detected, so as to react hydrogenation products in whole hydrogenation system
The content situation of the crystal salt blocked with the possibility in the fluid oil isolated.Therefore this method can real-time online detection can
The concentration for the crystal salt that can be blocked, so that more than 50 times that water injection rate is each tamper saturated concentration water requirement are controlled, one
Aspect is completely dissolved the crystal in pipeline and setting, controls it not crystallize as far as possible, on the other hand, due to the complexity of system
Property, the failure of change or system part of the crystal in some pipelines or reactor due to temperature and pressure may also be at certain
Partially crystallizable can occur for a little positions, in addition, the possibility that other solid matters precipitate also inevitably is had in system, this
The crystallization that inventing rational water injection rate can ensure to produce all is dissolved, while can also will likely produce the other of blocking
Insoluble matter develops, and realizes the complete removing to each blocking material.The species of salt probably from feedstock when may determine that
Come, when device is just run, for the silt, iron rust in system when tamper is less, water injection rate is 50-800 times, and water injection rate one is
In view of needing the concentration by salt to fall farther below saturated concentration, to avoid the possibility of crystallization, furthermore crystallization is allowed for
The ion of saline solution, such as Cl-, NO3Equipment can be caused to corrode, so its concentration is dropped to dilute enough；-When device is transported
Row is more than half a year, it is necessary to which more water are rinsed out, it is necessary to inject 800-1500 times when silt, iron rust tamper are more
Water.
This method real-time online understands tamper situation, continuous water filling, in time, fully removes among production phase oil
Tamper in product, while the size of the situation adjusting water injection rate according to the crystal salt for being easiest to block, cost is controllable, saves
Use water.Location of water injection be distributed in hydrogenation piece-rate system before, composition piece-rate system separator between so that hydrogenation products flow through
The pipeline that blocks of possibility and equipment rinsed, blocking position is completely covered so that among isolated fluid oil
Nitrogen, content of beary metal in product reduce.
The sensor receives the concentration signal that concentration sensor is sent and adjusts the valve to control water injection rate.
It is big in water injection rate and noted according to by the dimension scale and water injection rate of the equipment of water filling and pipeline and water injecting pipeline
When water lines are smaller, more water injecting pipelines are set, with rational deployment water injecting pipeline, are mitigated to by the impact of water injecting pipeline while reality
Now more preferable flushing effect.
The method of crystal salt is directed to slurry bed system hydrogenation technique in a kind of monitoring of the present invention and removing hydrogenation plant and pipeline
The problem of amount of the accessory substances such as the crystalline material generated after middle hydrogenation reaction is big, designs the wastewater outlet in last separator
Set concentration monitoring device to monitor crystal content in real time, and water injection rate is controlled according to concentration, multiple location of water injection are set, in time prison
The tamper in hydrogenation plant and pipeline is surveyed and removed, overcomes it to deposit on tube wall and blocks pipeline, to equipment and pump valve
Cause to wear, cause the adverse consequences such as shut-down, solve above-mentioned technical problem.
Brief description of the drawings
Fig. 1 is the embodiment schematic diagram of tamper in the piece-rate system in the removing slurry bed system hydrogenation technique of the present invention.
Each label lists as follows in figure：
1- high-temperature high-pressure separators, 2- medium temperature high-pressure separators, 3- normal temperature high voltage separators, 4- low-voltage high-temperature separators,
5- low pressure medium temperature separators, 6- low pressure normal temperature separators, 7- reaction products, 8- cooling agents, 9- desalted waters, 10- circulating hydrogens,
11- tail gas, 12- room temperature oil, 13- waste water, 14- medium temperatures oil, 15- high temperature oils.
Embodiment
For the technology contents that the present invention is further explained, will be illustrated with reference to the drawings and specific embodiments.
As shown in Figure 1, method of the present embodiment for the tamper in removing high pressure piece-rate system, piece-rate system belong to slurry
Separating technology in bed hydroprocessing reaction process.High pressure piece-rate system is made of six different separators, is respectively high temperature and pressure
Separator 1, medium temperature high-pressure separator 2, normal temperature high voltage separator 3, low-voltage high-temperature separator 4, low pressure medium temperature separator 5 and low pressure
Normal temperature separator 6.The Room-temperature low-pressure separator 6 is placed for horizontal type level, remaining separator is vertical vertical placement.To reach
The tampers such as the crystal salt in slurry reactor equipment and pipeline are removed, it is necessary to select suitable water quality, water temperature, hydraulic pressure, water filling
Point, in addition, will also determine water injection rate according to the solubility of crystalline material in water, ensure that its concentration is dense far below saturation
Degree.Pipeline of the location of water injection of the present embodiment between separator, there is provided two location of water injection, first location of water injection
Filling pipe connects the pipeline between high-temperature high-pressure separator 1 and medium temperature high-pressure separator 2；The note of second location of water injection
Pipeline between waterpipe connection medium temperature high-pressure separator 2 and normal temperature high voltage separator 3, with remove may contain in pipeline it is stifled
Plug thing.
In order to monitor the distribution situation of the tamper such as crystal salt in the concentration of waste water and waste water, and Reasonable Regulation And Control water filling in real time
Amount, waste water resource does not realize good removal effect at the same time, and the present embodiment is set in 6 wastewater outlet pipeline of Room-temperature low-pressure separator
Concentration detector (DEN) is put, while sensor and valve are set on filling pipe, the concentration detector and each filling pipe
On sensor connection.The concentration detector can detect that the density of crystal salt in waste water, then pass to concentration signal
Sensor on filling pipe, adjusts water injection valve.
In the present embodiment, when temperature is 50 DEG C, during DEN=1.36kg/l, salt is judged for sodium chloride, potassium chloride, correspondence
Concentration for 27wt%, it is necessary to by concentration dilution to 0.03wt%, corresponding DEN is 1.01kg/l at this time, when water injection rate reaches
When can make DEN=1.01kg/l, water injection rate is suitable.Wet concentration desalted water is injected, temperature is 40 DEG C, pressure 20MPa, is adjusted
Water injection rate is about 500 times of crystal saturated concentration in water.
So in the case where water consumption keeps less, big corrosion will not be caused to equipment.
The technique of conventional desalination：1st, water consumption is big, 2, wastewater treatment load it is excessive, it will usually more than design load, safety
Hidden danger is big, and production cost is high.
The tampers such as the crystal salt in the pipeline between separator in the removing slurry bed system hydrogenation technique of the present embodiment
Workflow is as follows：
Reaction product 7 enters high-temperature high-pressure separator 1 after cooling agent 8 is cooled to, and operation temperature is 420 DEG C, operation pressure
Power is 18.7MPa, and the gas phase that 1 top of high-temperature high-pressure separator is isolated enters medium temperature high-pressure separator 2 after cooling, water filling,
Liquid phase enters high-temperature low-pressure separator 4 after Liquid level valve regulation.Water injection rate ensures high-temperature high-pressure separator 1 and medium temperature high pressure
The crystal salt in pipeline between separator 2, which is dissolved, to be taken away, while is ensured that insoluble matter is rinsed and taken away, while after ensureing water filling
Gas phase media temperature be not less than 250 DEG C.2 operation temperature of medium temperature high-pressure separator is 285 DEG C, and operating pressure is 18.6MPa, on
The gas phase that part separates out enters normal temperature high voltage separator 3 after cooling down, noting desalted water 9 and secondary cooling, and liquid phase is through Liquid level
Enter medium temperature low pressure separator 5 after valve regulation, water injection rate used ensure medium temperature high-pressure separator 2 and normal temperature high voltage separator 3 it
Between pipeline in crystal salt be dissolved and take away, while ensure that insoluble matter is rinsed and take away.3 operation temperature of normal temperature high voltage separator
It it is 55 DEG C, operating pressure is 18.5MPa, and the gas phase that top is isolated is used as circulating hydrogen 10, under normal temperature high voltage separator 3
The liquid phase in portion enters Room-temperature low-pressure separator 6 after Liquid level valve regulation；4 operation temperature of high-temperature low-pressure separator is 420 DEG C,
Operating pressure is 3.0MPa, and the gas phase that top is isolated enters medium temperature low pressure separator 5 after cooling, and liquid phase is through fluid level control valve
Go out piece-rate system as high temperature oil 15 after adjusting；5 operation temperature of medium temperature low pressure separator is 285 DEG C, and operating pressure is 2.9MPa,
Upper gaseous phase enters Room-temperature low-pressure separator 6 after cooling, and liquid phase goes out separation after Liquid level valve regulation as medium temperature oil 14
System；6 operation temperature of Room-temperature low-pressure separator is 55 DEG C, and operating pressure is 2.8MPa, and upper gaseous phase goes out separation as tail gas 11
System enters gas treatment equipment, and lower liquid phase goes out piece-rate system as room temperature oil 12, in liquid collecting bag containing crystalline material and its
The waste water 13 of its accessory substance removes wastewater treatment equipment.Verified by accumulation up to 6000 pilot scales when small, nothing in each equipment and pipeline
Clogging, it is possible to achieve the long period of device is continuously run.
Certainly the method for the present invention also can also be set according to actual conditions, if being blocked in separator on separator
Filling pipe is put, rinses the tampers such as crystal salt in it.Or also can be before hydrogenation reaction product enters piece-rate system i.e.
Filling pipe is set in pipeline before high-temperature high-pressure separator 1.
The removal methods of the present invention can also be applied in conventional hydrogenation process, remove the blocking in hydrogenation plant and pipeline
Thing, dissolving crystallized thing, rinses out insoluble matter.
From above-described embodiment as can be seen that using the method for crystal salt in a kind of removing hydrogenation plant and pipeline of the invention
Real time and on line monitoring waste water situation, and according to tamper concentration and species reasonably select desalted water, suitable water temperature and hydraulic pressure,
Water injection rate is 50-1500 times of each crystal salt saturated concentration, sets multiple location of water injection to remove in time in hydrogenation plant and pipeline
Fall tamper, it is accurate control, easy to operate and practical.Can be by there may be blocking in product after slurry bed system hydrogenation reaction
Material separate, avoid block pipeline, cause to stop work.
Claims (8)
- A kind of 1. method for removing crystal salt in hydrogenation plant and pipeline, it is characterised in that at least in the useless of afterbody separator Concentration detector is set in water exit conduit, detects the concentration of crystal salt in the waste water converged after location of water injection water filling is rinsed, so The crystal salt element species in crystallization salinity, temperature and raw material judge crystal salt species and control location of water injection afterwards Water injection rate；Pipe between pipeline and/or separator and/or separator of the location of water injection between reactor and separator Road, when temperature be 50 DEG C, when the numerical value of concentration detector is 1.36kg/l, judge salt for sodium chloride, potassium chloride, corresponding concentration For 27wt%, it is necessary to by concentration dilution to 0.03wt%, adjust water injection rate for crystal salt in water saturated concentration water consumption 500 Times, the reactor and separator are used in heavy oil hydrogenation process, direct coal liquefaction process and oily coal calendering process, the heavy oil Hydrogenation technique refers to be combined as raw material and is processed with the one or more of residual oil, catalytic slurry, de-oiled asphalt, coal tar；Institute State oily coal calendering process refer to one or more kinds of combinations in crude oil, residual oil, catalytic slurry, de-oiled asphalt and coal tar with it is brown One or more in coal, bituminous coal are combined as raw material and are processed, and the proportion of oil and coal is 97-30:3-70.
- 2. according to the method described in claim 1, it is characterized in that separator contact successively including light fraction outlet, temperature successively Multiple normal pressures that the multiple high-pressure separators and light fraction outlet corresponding with high-pressure separator reduced are contacted successively separate Device, the light fraction outlet of the restructuring sub-export of each high-pressure separator normal pressure separator identical with corresponding temperature communicate.
- 3. according to the method described in claim 2, it is characterized in that separator include contact successively high-temperature high-pressure separator, in Warm high-pressure separator, normal temperature high voltage separator, and low-voltage high-temperature separator, low pressure medium temperature separator and the low pressure contacted successively Normal temperature separator, location of water injection be respectively the high-temperature high-pressure separator entrance before pipeline, each high-pressure separator Between pipeline, the afterbody separator is normal temperature and pressure separator.
- 4. according to any methods of claim 1-3, it is characterised in that set on the pipeline after water filling flushing valve and Sensor, the sensor are connected with the concentration detector.
- 5. according to the method described in claim 4, it is characterized in that the valve is internally piloted valve and/or hand valve.
- 6. according to the method described in claim 1, it is characterized in that there is 1-8 water injecting pipeline in each location of water injection.
- 7. according to the method described in claim 1, it is characterized in that the injection water quality is desalted water.
- 8. according to the method described in claim 1, it is characterized in that water filling temperature be 15-200 DEG C, pressure 1.0-25.0MPa.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510696047.0A CN105273759B (en) | 2015-10-23 | 2015-10-23 | A kind of method and its design method and purposes for removing crystal salt |
| PCT/CN2015/094113 WO2017067025A1 (en) | 2015-10-23 | 2015-11-09 | Method for removing crystalline salt, and design method and application thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510696047.0A CN105273759B (en) | 2015-10-23 | 2015-10-23 | A kind of method and its design method and purposes for removing crystal salt |
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| CN105273759A CN105273759A (en) | 2016-01-27 |
| CN105273759B true CN105273759B (en) | 2018-04-17 |
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| WO (1) | WO2017067025A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110215742A (en) * | 2018-03-01 | 2019-09-10 | 中石化广州工程有限公司 | A kind of method of hydrogenation plant dechlorination |
| CN110218580A (en) * | 2018-03-01 | 2019-09-10 | 中石化广州工程有限公司 | A kind of method of hydrogenation reaction effluent dechlorination |
| CN108275822A (en) * | 2018-03-20 | 2018-07-13 | 山东奥能电力科技有限公司 | A kind of dense salt waste water atomization concentration cycles crystallization Zero discharging system and technique |
| CN111040815B (en) * | 2019-12-18 | 2022-04-12 | 大连福佳·大化石油化工有限公司 | Desalting and corrosion preventing system of depentanizer |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101880543A (en) * | 2010-07-02 | 2010-11-10 | 沈阳石蜡化工有限公司 | Online cleaning method of deposited salt of tower tray of normal-pressure tower |
| US20100292106A1 (en) * | 2007-11-13 | 2010-11-18 | Akzo Nobel N.V. | Methods of minimizing sulfate scale in oil field |
| CN104845664A (en) * | 2015-05-08 | 2015-08-19 | 北京中科诚毅科技发展有限公司 | Multiple-optimizing separator combined systems as well as use method and design method |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE60135162D1 (en) * | 2001-10-03 | 2008-09-11 | Pierre Descloux | PROCESS FOR PREPARING CORROSION AND DEPOSITS IN A HOT WATER SYSTEM AND DEVICE FOR CARRYING OUT THE METHOD |
| CN101655336B (en) * | 2009-07-27 | 2011-01-12 | 浙江理工大学 | Optimization method of water injection for hydrogenation reaction outflow air-cooler system |
| CN101639688B (en) * | 2009-08-17 | 2011-05-18 | 浙江理工大学 | Optimization method of hydrogenation reaction effluent air cooler system for preventing erosion of NH4HS |
| CN104808614A (en) * | 2015-03-02 | 2015-07-29 | 浙江理工大学 | Hydrogenation reaction effluent air cooler system optimization method for preventing NH4Cl under-deposit corrosion |
-
2015
- 2015-10-23 CN CN201510696047.0A patent/CN105273759B/en active Active
- 2015-11-09 WO PCT/CN2015/094113 patent/WO2017067025A1/en active Application Filing
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100292106A1 (en) * | 2007-11-13 | 2010-11-18 | Akzo Nobel N.V. | Methods of minimizing sulfate scale in oil field |
| CN101880543A (en) * | 2010-07-02 | 2010-11-10 | 沈阳石蜡化工有限公司 | Online cleaning method of deposited salt of tower tray of normal-pressure tower |
| CN104845664A (en) * | 2015-05-08 | 2015-08-19 | 北京中科诚毅科技发展有限公司 | Multiple-optimizing separator combined systems as well as use method and design method |
Non-Patent Citations (1)
| Title |
|---|
| "加氢处理系统NH4Cl结晶沉积预测及优化防控";金浩哲等;《石油学报(石油加工)》;20140831;第30卷(第4期);第662-667页 * |
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| CN105273759A (en) | 2016-01-27 |
| WO2017067025A1 (en) | 2017-04-27 |
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