CN101654626A - Cyclone separation technology used for on-line separation of hydrocarbons and solid granules in desulfurized solvent - Google Patents
Cyclone separation technology used for on-line separation of hydrocarbons and solid granules in desulfurized solvent Download PDFInfo
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- CN101654626A CN101654626A CN200810139247A CN200810139247A CN101654626A CN 101654626 A CN101654626 A CN 101654626A CN 200810139247 A CN200810139247 A CN 200810139247A CN 200810139247 A CN200810139247 A CN 200810139247A CN 101654626 A CN101654626 A CN 101654626A
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- cyclone separator
- desulfurization solvent
- solvent
- hydro carbons
- desulfurized
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Abstract
The invention discloses cyclone separation technology used for on-line separation of hydrocarbons and solid granules in a desulfurized solvent in a gas desulfurization device, which belongs to the processing field of petroleum and natural gas. Mainly aiming at the characteristics of the hydrocarbons and the solid granules in the desulfurized solvent, the technology removes a large part of hydrocarbons and solid granules in the desulfurized solvent by a method of increasing a cyclone separator and a filter in front of a desulfurized solvent flash pot in the processing technique of the conventional gas desulfurization device so as to effectively reduce or avoid the desulfurized solvent foaming in a regenerating tower, reduce energy consumption and agent consumption and reclaim the part of hydrocarbon substances at the same time of providing protection for normal production of a desulfurized solvent purifying system and a downstream sulfur production device.
Description
Technical field
The invention belongs to the refining of petroleum field, particularly the improvement of gas sweetening unit complete processing.
Background technology
In the sulphur-bearing crude secondary processing process of refining of petroleum field, sizable a part of sulphur is converted into hydrogen sulfide in the crude oil.During as petrochemical materials or fuel, causing the corrosion of chemical production equipment and pipeline with the sulfurous gas of such character, cause poisoning of catalyst, also pollute the environment simultaneously, be detrimental to health.In addition, the hydrogen sulfide in the gas also is to make sulphur and vitriolic raw material.Therefore hydrogen sulfide stripping in the refinery gas need be re-used as raw material or fuel that petrochemical complex is produced.
The most of refinery gas gas sweetening unit of China adopts the chemical absorption method desulfurization, promptly use and carry out chemical absorption with the alkaline matter of hydrogen sulfide reaction (as diethanolamine etc.) and receive, the desulfurization solvent that has absorbed hydrogen sulfide is deviate from hydrogen sulfide by the method for step-down, heating in the desulfurization solvent regenerator column.
Process of desulfurizing gases is in the prior art:
The advanced hydrogen sulfide absorption tower of hydrogen sulfide containing refinery gas, cat head is discharged and is removed the gas of hydrogen sulfide as petrochemical materials or fuel, discharge at the bottom of the tower when the laggard flash tank of desulfurization solvent (the refining of petroleum industry is commonly referred to rich solution) step-down absorbed hydrogen sulfide flashes off part low boiling point hydrocarbon (gas phase) and rely on gravity settling separation to go out the higher hydro carbons of part boiling point (liquid phase), enter the desulfurization solvent regenerator column then.The regenerator column cat head is discharged the sour gas desulfuration sulphur device that contains high-concentration hydrogen sulfide and is produced sulphur, discharge regeneration back desulfurization solvent (the refining of petroleum industry is commonly referred to lean solution) at the bottom of the tower and divide two-way, one the tunnel directly advances storage tank, and another road (accounting for the 15-20% of total flux) goes the desulfurization solvent purification system.These desulfurization solvents are the solid particulate in mechanical filter removal desulfurization solvent earlier, remove hydro carbons and degraded product through the activated carbon adsorption strainer again, enter the desulfurization solvent storage tank after removing the solid particulates such as activated carbon that bring the upstream through a mechanical filter more at last.
The flash tank design residence time is generally less than 20 minutes, and the actual residence time of partial devices was less than 10 minutes.
Because the solid particulates such as Iron sulfuret that hydrocarbon liquids in the refinery gas and corrosion produce can't all remove in upstream device, these materials major part when refinery gas process hydrogen sulfide absorption tower enters in the desulfurization solvent (the refining of petroleum industry is commonly referred to rich solution) that has absorbed hydrogen sulfide.
Hydrocarbons in the desulfurization solvent is divided into four kinds of states by granular size: suspension, dispersion, emulsification, dissolving, corresponding particle size distribution is: (with 60 microns is the boundary greater than 100 microns, 15～100 microns, be not more than finely divided hydro carbons of 60 microns be called, greater than 60 microns be called the rough segmentation hydro carbons that looses), 0.5～15 micron, less than 0.5 micron.For suspension hydro carbons and the rough segmentation hydro carbons that looses, generally use the conventional slurry tank (settling time is longer, is generally several hrs) can effective collection; For finely divided hydro carbons, also can reclaim by long-time (being generally several days) gravity settling greater than 30 micron particle, but the particle of 15-30 micron is difficult to reclaim; For the emulsified state hydro carbons, the application of weight separation method is difficult to remove, and generally adopts the air supporting choosing method; For the dissolving hydro carbons, adopt physical method to be difficult to reclaim, generally adopt biochemical process to remove.
Hydro carbons in the desulfurization solvent is mainly suspension, dispersion, emulsified state hydro carbons.
Solid particulate in the desulfurization solvent is mainly Iron sulfuret that corrosion produces and iron filings etc., these solid particulate major parts are suspended in the desulfurization solvent, density is greater than desulfurization solvent, can remove by the gravity separation method, but also some solid particulate and hydro carbons combine, density and desulfurization solvent are suitable, can't remove by the gravity separation method.
Because hydro carbons and solid particulate diameter less (major part is 5～100 microns) in the desulfurization solvent, and flash tank liquid is in flow state always, it is very low that flash tank removes in the desulfurization solvent efficient of hydro carbons and solid particulate matter, hydrocarbons content is still greater than 1000PPM in a lot of device desulfurization solvent flash tanks outlet desulfurization solvents, thereby brings a series of problems:
1, desulfurization solvent blackout, foaming: it is black when waiting solid particulate and hydrocarbon liquids that Containing Sulfur is ferrous in the desulfurization solvent, (mechanical product such as Iron sulfuret is the inducement of foaming in foaming also can to cause desulfurization solvent (as diethanolamine etc.) in addition when solid particulate such as Iron sulfuret and hydrocarbon liquids exist simultaneously, hydro carbons is actual foaming substance), thus the normal operation of desulfurization solvent regenerator column influenced;
2, hydrocarbon content exceeds standard (the highest hydrocarbon content surpasses 10%) in the solvent reclamation column overhead sour gas, and it is undesired that the downstream sulphur production installation is produced: because the sour gas calorific value is 3.54GJ/m
3And the calorific value of hydro carbons is about sour gas calorific value twelvefold, difference of them is bigger, the cat head sour gas that contains the higher concentration hydro carbons enters the downstream sulphur unit can cause this device furnace temperature to be difficult to control, conversion system can't be kept autothermal equilibrium, equipment corrodes, product defective (it is black to produce sulphur), and device can't ordinary production.
3, sour gas is taken away a large amount of hydro carbons, and the enterprise refining losses increases: with hydro carbons concentration 10% (weight) in the sour gas, producing 40000 tons of sulphur production installations per year is example, and the hydro carbons that 1 year sour gas is taken away is about 4000 tons.
4, regeneration back desulfurization solvent purification system can't normally be moved, and is forced to replace in a large number desulfurization solvent or changes desulfurization solvent, has increased the loss of desulfurization solvent when easily causing environmental pollution greatly.Since regeneration Tata at the bottom of liquid be in state of disturbance always and the residence time not enough, enter higher hydro carbons of most of boiling point at the bottom of the tower and solid particulate with tower at the bottom of regeneration back desulfurization solvent enter the desulfurization solvent purification system, the content of these hydro carbons and solid particulate substantially exceeds the adsorptive power of activated carbon adsorption strainer, cause this strainer and can't come into operation because back flushing is too frequent, the long-term by-passing of desulfurization solvent, the desulfurization solvent quality obviously descends in the system, be forced to system's internal solvent is replaced or changed, bring environmental problem when causing the agent consumption to increase;
5, increase the regenerator column power consumption: enter with desulfurization solvent that the low component of part boiling point is in the circulation of regenerator column internal system in the hydro carbons of regenerator column, this will increase the energy consumption of regenerator column.
Summary of the invention
Purpose of the present invention provides a kind of cyclone separation process that is used for ON-LINE SEPARATION gas sweetening unit desulfurization solvent hydrocarbons and solid particulate with regard to being to avoid above-mentioned the deficiencies in the prior art part, this technology mainly is the characteristics at hydrocarbons in the desulfurization solvent and solid particulate, by increasing the online most of hydro carbons and the solid particulate that removes in the desulfurization solvent of method of cyclone separator and strainer before the desulfurization solvent flash tank in conventional gas sulfur removal technology process, effectively reduce or avoid desulfurization solvent to foam at regenerator column, cut down the consumption of energy, agent consumption reclaims this part hydrocarbons when providing safeguard for desulfurization solvent purification system and downstream sulphur production installation ordinary production.
Description of drawings
Accompanying drawing is process flow sheet of the present invention
The drawing of accompanying drawing is described as follows:
1, gas sweetening tower (T-1) 2, cyclone separator (Y-1)
3, desulfurization solvent flash tank (V-1) 4, strainer (F-1)
5, desulfurization solvent regenerator column (T-2) 6, sour gas divide flow container (V-2)
7, sulphur production installation (M-1) 8, interchanger (E-1)
9, reboiler (E-2) 10, hydro carbons holding tank (V-3)
11, encloses container (V-4)
Embodiment
Technical characterstic of the present invention and effect are described in detail in detail below in conjunction with specific embodiments:
According to technical process shown in the accompanying drawing, the sulfide hydrogen refinery gas enters hydrogen sulfide absorption tower (T-1) from the bottom, gas contacts with the sweetening agent that enters from the top is reverse in tower, the desulfurization solvent (the refining of petroleum industry is commonly referred to rich solution) that has absorbed hydrogen sulfide is discharged from hydrogen sulfide absorption tower (T-1) bottom, be introduced into the interior cyclone separator of encloses container (V-4) (Y-1), adopt existing cyclone separation process to isolate part solid particulate and the hydro carbons of particle diameter more than 10 microns of carrying secretly in the desulfurization solvent, cyclone separator (Y-1) is isolated hydro carbons and is collected into hydro carbons holding tank (V-2) automatically or directly drains into oil skimming tank, the solid particulate that is deposited in encloses container (V-4) bottom cone utilizes hydraulic effect operated valve discharge manually at any time (perhaps electrically operated valve is regularly discharged automatically), requires per tour to open once; The desulfurization solvent that comes out from encloses container (V-4) top pass through again filter (F-1) remove most of combining with hydro carbons can't be by behind the solid particulate of spinning liquid separation removal, enter desulfurization solvent flash tank (V-1), flash distillation after desulfurization solvent and the regeneration back sweetening agent heat exchange at the bottom of desulfurization solvent regenerator column (T-2) tower of dissolved hydrocarbon, enter desulfurization solvent regenerator column (T-2) from the top, the sour gas that removes out is introduced into branch flow container (V-2) remove the drops such as water carry secretly after desulfuration sulphur production equipment (M-1) produce sulphur.
Through after the above art breading, the hydrocarbon liquids particle major part of particle diameter more than 20 microns removed in the desulfurization solvent, and hydrocarbon content is stabilized in 150PPm following (not comprising emulsifying hydrocarbon and dissolved hydrocarbon); Hydrocarbon content is less than 3.5% (weight) in the desulfurization solvent regeneration overhead sour gas.
Technical characterstic of the present invention is different from the conventional gas sulfur removal technology, and it has following features:
1. adopt rotational flow separation combine with filtering technique most of hydro carbons and solid particle in the ON-LINE SEPARATION desulfurization solvent, technology Technology and equipment are simple, except increasing a cyclone separator, hydro carbons collecting tank and a cover filtration system, need not other additional equipments, Investment cost is low;
2. cyclone separator is told hydro carbons and is adopted automatic drain, reduces labor intensity of operating staff;
3. cyclone separator is told and can be carried out freshening again after hydro carbons enters the hydro carbons holding tank, increases the benefit of oil and gas processing enterprise.
Claims (9)
1, a kind of cyclone separation process that is used for ON-LINE SEPARATION gas sweetening unit desulfurization solvent hydro carbons and solid particulate, it mainly is to have adopted in conventional gas sulfur removal technology process to increase cyclone separator and strainer before the desulfurization solvent flash tank and realize the online most of hydro carbons in the desulfurization solvent and the method for solid particulate of removing.It is characterized in that this method follows these steps to realize: by increasing the online most of hydro carbons and the solid particulate that removes in the desulfurization solvent of method of single-stage or multistage liquid liquid cyclone separator and strainer before the desulfurization solvent flash tank in conventional gas sulfur removal technology process, the operational condition of cyclone separator is: temperature: 30-100 degree centigrade, and pressure: 0.1-5.0Mpa.
2, method according to claim 1 is characterized in that: above-mentioned cyclone separation process can increase cyclone separator and strainer before the desulfurization solvent flash tank, also can increase cyclone separator before the desulfurization solvent flash tank and does not establish strainer.
3, method according to claim 1 is characterized in that: described cyclone separator can be the multitubular bundles cone shape cyclone separator in the prior art, also can be single tube cone shape cyclone separator.
4, method according to claim 1 is characterized in that: what described cyclone separator adopted can be the single-stage cyclone separator.
5, according to claim 1 it is characterized in that: what described cyclone separator adopted can be multistage cyclone separator.
6, method according to claim 1 is characterized in that: described cyclone separator is selected from hydrocyclone, whirlwind-type cyclone separator, coarse cyclone separator and eddy flow-jet-coarse cyclone separator.
7, method according to claim 1 is characterized in that: described cyclone separator and strainer are arranged at before the desulfurization solvent flash tank.
8, method according to claim 1 is characterized in that: described cyclone separator is isolated hydro carbons can collect the hydro carbons holding tank, also can directly drain into oil skimming tank.
9, method according to claim 1 is characterized in that: in the vertebra shape chamber, can manually regularly discharge at the bottom of described cyclone separator is isolated solid particulate and is deposited in earlier jar, also can regularly discharge automatically.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810139247A CN101654626A (en) | 2008-08-21 | 2008-08-21 | Cyclone separation technology used for on-line separation of hydrocarbons and solid granules in desulfurized solvent |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810139247A CN101654626A (en) | 2008-08-21 | 2008-08-21 | Cyclone separation technology used for on-line separation of hydrocarbons and solid granules in desulfurized solvent |
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| CN101654626A true CN101654626A (en) | 2010-02-24 |
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| CN200810139247A Pending CN101654626A (en) | 2008-08-21 | 2008-08-21 | Cyclone separation technology used for on-line separation of hydrocarbons and solid granules in desulfurized solvent |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105883730A (en) * | 2016-05-05 | 2016-08-24 | 中钛集团洛阳市裕星化工有限公司 | Method for concentrating waste acid in titanium dioxide production based on sulfuric acid process |
| CN108786376A (en) * | 2017-04-28 | 2018-11-13 | 中国石化工程建设有限公司 | A kind of method and system of recycling volatile organic matter |
| CN109954289A (en) * | 2017-12-22 | 2019-07-02 | 上海华畅环保设备发展有限公司 | Desulfurization rich amine solution eddy flow strengthens de- hydrocarbon method and apparatus |
-
2008
- 2008-08-21 CN CN200810139247A patent/CN101654626A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105883730A (en) * | 2016-05-05 | 2016-08-24 | 中钛集团洛阳市裕星化工有限公司 | Method for concentrating waste acid in titanium dioxide production based on sulfuric acid process |
| CN105883730B (en) * | 2016-05-05 | 2018-01-19 | 焦作市裕盛钛业有限公司 | A kind of method of waste acid concentration in sulfuric acid method titanium pigment production |
| CN108786376A (en) * | 2017-04-28 | 2018-11-13 | 中国石化工程建设有限公司 | A kind of method and system of recycling volatile organic matter |
| CN109954289A (en) * | 2017-12-22 | 2019-07-02 | 上海华畅环保设备发展有限公司 | Desulfurization rich amine solution eddy flow strengthens de- hydrocarbon method and apparatus |
| CN109954289B (en) * | 2017-12-22 | 2021-08-27 | 镇海石化工程股份有限公司 | Desulfurization amine-rich liquid cyclone reinforced dealkylation method and device |
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Open date: 20100224 |