CN104193034B - A kind of amine purification processes system - Google Patents
A kind of amine purification processes system Download PDFInfo
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- CN104193034B CN104193034B CN201410461234.6A CN201410461234A CN104193034B CN 104193034 B CN104193034 B CN 104193034B CN 201410461234 A CN201410461234 A CN 201410461234A CN 104193034 B CN104193034 B CN 104193034B
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- elimination
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- amine
- heat stable
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- 150000001412 amines Chemical class 0.000 title claims abstract description 62
- 238000000746 purification Methods 0.000 title claims abstract description 17
- 230000008030 elimination Effects 0.000 claims abstract description 63
- 238000003379 elimination reaction Methods 0.000 claims abstract description 63
- 239000007788 liquid Substances 0.000 claims abstract description 52
- 150000001768 cations Chemical class 0.000 claims abstract description 50
- 239000002184 metal Substances 0.000 claims abstract description 40
- 229910052751 metal Inorganic materials 0.000 claims abstract description 40
- -1 salt anion Chemical class 0.000 claims abstract description 28
- 238000000034 method Methods 0.000 claims abstract description 15
- 239000012530 fluid Substances 0.000 claims abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 230000008569 process Effects 0.000 claims abstract description 6
- 125000002091 cationic group Chemical group 0.000 claims description 9
- 239000002253 acid Substances 0.000 claims description 8
- 239000011347 resin Substances 0.000 claims description 8
- 229920005989 resin Polymers 0.000 claims description 8
- 229920006395 saturated elastomer Polymers 0.000 claims description 5
- 239000007789 gas Substances 0.000 description 13
- 238000004140 cleaning Methods 0.000 description 9
- 230000008929 regeneration Effects 0.000 description 8
- 238000011069 regeneration method Methods 0.000 description 8
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- 239000003513 alkali Substances 0.000 description 4
- 239000003729 cation exchange resin Substances 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 4
- QZAYGJVTTNCVMB-UHFFFAOYSA-N serotonin Chemical compound C1=C(O)C=C2C(CCN)=CNC2=C1 QZAYGJVTTNCVMB-UHFFFAOYSA-N 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 3
- 230000035508 accumulation Effects 0.000 description 3
- 230000002411 adverse Effects 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 238000005187 foaming Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 150000001450 anions Chemical class 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- PCHPORCSPXIHLZ-UHFFFAOYSA-N diphenhydramine hydrochloride Chemical compound [Cl-].C=1C=CC=CC=1C(OCC[NH+](C)C)C1=CC=CC=C1 PCHPORCSPXIHLZ-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- 239000003957 anion exchange resin Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000011981 development test Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000008258 liquid foam Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000010525 oxidative degradation reaction Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Removal Of Specific Substances (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The present invention relates to a kind of amine purification and process system, including elimination float system, elimination heat stable salt anion system, remove metal cation system and circulation fluid case and the recycle liquid pump being attached thereto; It is sequentially connected with by pipeline between elimination float system, elimination heat stable salt anion system and elimination metal cation system, circulation fluid case is connected with demineralized water supply pipeline and recycle liquid pump with valve respectively by pipeline, and recycle liquid pump is connected with the elimination heat stable salt anion tank in the elimination float tank in elimination float system, elimination heat stable salt anion system and the elimination metal cation tank in elimination metal cation system with valve respectively by pipeline. Amine liquid after being processed by present system, it is possible to the metal cation level in amine liquid system is reduced to normal level, is conducive to the stable operation of desulfurizer.
Description
Technical field
The present invention relates to a kind of amine purification and process system, particularly to the cleaning treatment system of the amine liquid used in the sulfur removal technology of oil plant and natural gas plant.
Background technology
In oil and gas processing gas purification process, adopting hydramine method desulfurization and decarburization is a kind of of paramount importance method, and wherein the selective absorption technique of N methyldiethanol amine (MDEA) is current domestic most popular gas purifying technique. MDEA has the advantages that low energy consumption, low-corrosiveness and low degradation rate, has developed very rapid since coming out from the eighties in last century. So far the whole gas sweetening decarburization field of the application nearly cover of MDEA and formula solvent thereof.
The requirement purified recently as environmental protection and energy saving aspect is further strict, and the performance of gas cleaning plant and the prescription of amine liquid is also more and more higher. Owing to feeding gas is brought into and the reason such as the oxidative degradation of amine in hydramine sweetening process, bringing a series of harm to device: corrosion of equipment, amine liquid foams, and cleaning filter, changes frequently, simultaneously amine liquid run damage serious. Typical amine purification processing procedure has distillating recovering solvent at present, and adopts filtration, ion exchange to remove the method for impurity in amine liquid. Wherein the method for filtration+ion exchange is applied relatively broad greatly because of simple to operate, treating capacity. But common amine purification method considers the removal of solid suspension and thermal-stable salt, and have ignored the removal of strong cation in amine liquid.
Such as patent of invention 200810057069.2, disclose a kind of cleaning treatment system, be only provided with the device removing solid suspension and thermal-stable salt, it does not have remove cationic device. In amine liquid system due to unstripped gas carry, equipment corrosion etc. can cause a large amount of accumulations of metal cation in amine liquid. A large amount of existence of metal cation can cause problems with: gas product is defective, and exhaust emissions exceeds standard; Amine absorption and analyzing efficiency are low, and in lean solution, acid gas residual quantity is big, and device disposal ability declines; Shape scaling salt block system pipeline. Especially, after using anionexchangetechnique to remove the heat stable salt anion in amine liquid, the impact of metal cation particularly highlights, and therefore, the removal to metal cation is also the problem that can not be ignored. The present invention is the technological improvement development carried out on the basis of patent 200810057069.2.
Summary of the invention
The present invention is directed to the existing state of the art, it is provided that a kind of amine purification system, it is possible to remove the heat stable salt anion in amine liquid and metal cation simultaneously, make amine purification. The method can operate with the system of the problem caused in the devices such as alcohol amine desulfurization because of metal cation too high levels.
The object above of the present invention is achieved by the following technical solution:
A kind of amine purification processes system, including elimination float (SSX) system, elimination heat stable salt anion (HSSX) system, removes metal cation (SCX) system and circulation fluid case and the recycle liquid pump being attached thereto. It is sequentially connected with by pipeline between elimination float system, elimination heat stable salt anion system and elimination metal cation system, described circulation fluid case is connected with demineralized water supply pipeline and the recycle liquid pump from user with valve respectively by pipeline, and described recycle liquid pump is connected with the elimination heat stable salt anion tank in the elimination float tank in elimination float system, elimination heat stable salt anion system and the elimination metal cation tank in elimination metal cation system with valve respectively by pipeline.
This cleaning system comprises elimination metal cation system, and elimination metal cation system is placed in after removing heat stable salt anion system, adopting cationic resin in elimination metal cation (SCX) system, the acid solution that the cationic resin after saturated adopts mass concentration to be 3% regenerates. Amine liquid, after entrance system, first removes float and heat stable salt anion, enters back into SCX system and removes the metal cation in amine liquid by cation exchange resin.
Advantages of the present invention is as follows:
1. the amine liquid after being processed by SCX system, it is possible to the metal cation level in amine liquid system is reduced to normal level, is conducive to the stable operation of desulfurizer.
2. after elimination metal cation (SCX) system being placed in elimination heat stable salt anion (HSSX) system canister, it is possible to reduce cation exchange resin to the cationic absorption of amine.
3. the anion exchange aqueous slkali after saturated regenerates, cation exchange resin acid solution after saturated regenerates, the mixing of two kinds of regenerative wastewater can reduce the pH value of waste water so that it is more disposable after entering Waste Water Treatment, properly functioning without influence on waste water system.
Accompanying drawing explanation
Fig. 1 is the amine cleaning system flow chart of the present invention.
Detailed description of the invention
As it is shown in figure 1, be system structure signal and the flow chart of the present invention. Including elimination float (SSX) tank 1, elimination heat stable salt anion (HSSX) tank 2, elimination metal cation (SCX) tank 3 and circulation fluid case 4 and the recycle liquid pump 5 being attached thereto. It is sequentially connected with by pipeline between elimination float tank 1, elimination heat stable salt anion tank 2 and elimination metal cation tank 3, circulation fluid case 4 is connected with demineralized water supply pipeline and the recycle liquid pump 5 from user with valve respectively by pipeline, and recycle liquid pump 5 is connected with elimination float tank 1, elimination heat stable salt anion tank 2 and elimination metal cation tank 3 with valve respectively by pipeline.
This cleaning system comprises elimination metal cation tank 3, and elimination metal cation tank 3 is placed in after removing heat stable salt anion tank 2, adopting cationic resin in elimination metal cation (SCX) tank 3, the acid solution that the cationic resin after saturated adopts mass concentration to be 3% regenerates.
Purification process: non-purified amine liquid is introduced into elimination float (SSX) tank 1 to remove the solid impurity in amine liquid, the amine liquid of removing float enters back into elimination heat stable salt anion (HSSX) tank 2 and removes heat stable salt anion, subsequently entering the metal cation that elimination metal cation (SCX) tank 3 is removed in amine liquid, the purification amine liquid after elimination cation returns amine system.
After system runs a period of time, the float that SSX tank retains gets more and more, thus reducing its disposal ability. When SSX tank filtration yield reaches its setting value or inlet outlet pressure differential reaches setting value, it is necessary to SSX tank is carried out, to recover its operating flux.
1) row's amine is just washed
Circulation fluid enters SSX tank from SSX tank top forward, and adjustment flow is setting value, and the purification amine in SSX tank is pressed into user's amine pipeline. Circulation flushing SSX tank, rinses water outlet and changes and enter in cyclic water tank, to reduce the loss of amine.
2) backwash
Demineralized water adverse current enters SSX tank, and adjustment flow is setting value. When volume of intaking reaches setting value, SSX tank cleans and terminates, and can enter amine and start new circulation.
After HSSX tank and SCX tank run certain time, when the exchange capacity of alternative one reaches the amine liquid exchange capacity differential pressure of setting more than setting value, it is necessary to it is carried out Regeneration Treatment, makes it again possess deionizing ability.
1) row's amine is just washed
Circulation fluid forward enters HSSX tank and SCX tank, utilizes the solution in circulation fluid case 4 to be circulated cleaning, reduces the loss of amine.
2) regeneration
The flow regulating demineralized water is setting value, quantitative with amount of calculation pump, HSSX tank reversely pumps into the sodium hydroxide solution regeneration of 4% (quality), SCX tank reversely pumps into the hydrochloric acid solution of 3% (quality) and regenerates, and regenerated liquid adverse current enters in tank, so that resin can loosen and again arrange, regenerated liquid is made to be uniformly distributed, improve regeneration effect, when acid, alkali consumption reach setting value, regeneration ending.
3) displacement
After regeneration ending, stopping into acid, alkali liquor, continue adverse current and enter demineralized water, adjustment flow of inlet water is setting value, carries out replacement operator. The acid remained in the middle of resin, alkali liquor can be discharged by replacing. After water outlet conductance reaches setting value, replacement completion.
In regeneration and replacement process, alkali pump first starts than sour pump and stops afterwards, is alkalescence after keeping regeneration water outlet mixing.
4) just wash
Circulation fluid forward enters HSSX tank and SCX tank, is then refluxed for circulation fluid case. Adjustment flow is setting value, when running to setting value, is just washing end.
5) amine setting-out is entered
Amine liquid forward enters HSSX tank and SCX tank, and the replacing water in HSSX tank is pressed into circulation fluid case, when entering amine volume to setting value, stops setting-out, starts new circulation.
Embodiment:
In tower, I oil vapor treatment station belongs to oil vapor treatment station, first, I gas field development test block in Tarim Oilfield tower. There is two major features in natural gas ore deposit handled by this station: a, belong to Condensate Field; B, gas mineral water salinity are significantly high. Go into operation the initial stage in this station in October, 2010, a large amount of condensates enter amine liquid with unstripped gas, amine liquid is caused to pollute, amine liquid is muddy, band oil substantially, foaming is serious, cause flash distillation gas carrying liquid, absorption tower foaming to block liquid, liquid phase circulates freely, the problems such as liquid are blocked in regenerator foaming, even occurred that primary system stopped, and have impact on the stable operation of desulphurization system and desulfurized effect time serious.
This situation needs amine purifier except there to be heat stable salt and defecator in removal amine liquid, must also have the device processing amine liquid cationic simultaneously, otherwise be extremely difficult to intended purification target, even influence whether the stable operation of amine cleaning system.
In order to solve the problems referred to above, on the basis of elimination float (SSX) system and elimination heat stable salt anion (HSSX) system, adding elimination metal cation (SCX) system, assembly of the invention formally comes into operation in December, 2010 I oil vapor treatment station in tower.Coming into operation latter five days, amine liquid foamed phenomenon is effectively controlled, and desulphurization system amine liquid turbid phenomenon is improved. The operational effect of apparatus of the present invention refers to table 1, for the steady salt of heat in device portal and exit amine liquid, cation and anion test Data Comparison. Anion and cation exchange resin unit on this covering device serves good clean-up effect equally, effectively slow down equipment corrosion, it is therefore prevented that tower that in amine liquid, the accumulation of salinity causes, device equipment salification phenomenon.
Table 1
Amine liquid, after entrance system, first removes float and heat stable salt anion, enters back into elimination metal cation system and removes the metal cation in amine liquid by cation exchange resin. Owing to adding elimination metal cation system, it is possible to remove the metal cation in amine liquid system, effectively slow down equipment corrosion, it is therefore prevented that tower that in amine liquid, the accumulation of salinity causes, device equipment salification phenomenon, it is ensured that the stable operation of desulfurizer.
Claims (3)
1. an amine purification processes system, it is characterised in that: include elimination float system, elimination heat stable salt anion system, elimination metal cation system and circulation fluid case and the recycle liquid pump being attached thereto; It is sequentially connected with by pipeline between described elimination float system, elimination heat stable salt anion system and elimination metal cation system, described circulation fluid case is connected with demineralized water supply pipeline and recycle liquid pump with valve respectively by pipeline, and described recycle liquid pump is connected with the elimination heat stable salt anion tank in the elimination float tank in elimination float system, elimination heat stable salt anion system and the elimination metal cation tank in elimination metal cation system with valve respectively by pipeline.
2. amine purification according to claim 1 processes system, it is characterised in that: after described elimination metal cation system is placed in elimination heat stable salt anion system, elimination metal cation system adopts cationic resin.
3. amine purification according to claim 2 processes system, it is characterised in that: the acid solution adopting mass concentration to be 3% after described cationic resin is saturated regenerates.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410461234.6A CN104193034B (en) | 2014-09-11 | 2014-09-11 | A kind of amine purification processes system |
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| CN201410461234.6A CN104193034B (en) | 2014-09-11 | 2014-09-11 | A kind of amine purification processes system |
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| CN104193034B true CN104193034B (en) | 2016-06-08 |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106178591B (en) * | 2015-05-08 | 2019-03-15 | 北京思践通科技发展有限公司 | A method of purification organic amine |
| CN107930399A (en) * | 2017-11-21 | 2018-04-20 | 攀钢集团攀枝花钢铁研究院有限公司 | The removal methods of foreign ion in a kind of organic amine desulfuration solution |
| CN108392896A (en) * | 2018-05-07 | 2018-08-14 | 山东胜星化工有限公司 | A kind of amine liquid removes the control system of coke powder purifier |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101219815A (en) * | 2008-01-29 | 2008-07-16 | 王建军 | Cleaning treatment system |
| AU2008202311A1 (en) * | 2008-05-22 | 2009-12-10 | Al-Samadi, Riad Dr | High Water Recovery Single Stage Membrane Process |
| CN103979716A (en) * | 2014-05-22 | 2014-08-13 | 西安热工研究院有限公司 | System and method for purifying and recycling amine liquid of smoke CO2 trapping system for coal-fired power plant |
| CN204058129U (en) * | 2014-09-11 | 2014-12-31 | 王建军 | A kind of amine purification treatment system |
-
2014
- 2014-09-11 CN CN201410461234.6A patent/CN104193034B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101219815A (en) * | 2008-01-29 | 2008-07-16 | 王建军 | Cleaning treatment system |
| AU2008202311A1 (en) * | 2008-05-22 | 2009-12-10 | Al-Samadi, Riad Dr | High Water Recovery Single Stage Membrane Process |
| CN103979716A (en) * | 2014-05-22 | 2014-08-13 | 西安热工研究院有限公司 | System and method for purifying and recycling amine liquid of smoke CO2 trapping system for coal-fired power plant |
| CN204058129U (en) * | 2014-09-11 | 2014-12-31 | 王建军 | A kind of amine purification treatment system |
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