CN101973654A - Method for reducing dosage and discharge of flushing liquor for device of removing heat stable salts in solvent - Google Patents
Method for reducing dosage and discharge of flushing liquor for device of removing heat stable salts in solvent Download PDFInfo
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- CN101973654A CN101973654A CN2010102999322A CN201010299932A CN101973654A CN 101973654 A CN101973654 A CN 101973654A CN 2010102999322 A CN2010102999322 A CN 2010102999322A CN 201010299932 A CN201010299932 A CN 201010299932A CN 101973654 A CN101973654 A CN 101973654A
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- stable salts
- washing fluid
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- 150000003839 salts Chemical class 0.000 title claims abstract description 104
- 239000002904 solvent Substances 0.000 title claims abstract description 81
- 238000011010 flushing procedure Methods 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000002699 waste material Substances 0.000 claims abstract description 28
- 238000007599 discharging Methods 0.000 claims abstract description 26
- 239000012530 fluid Substances 0.000 claims description 135
- 238000005406 washing Methods 0.000 claims description 93
- 239000007788 liquid Substances 0.000 claims description 25
- 239000000243 solution Substances 0.000 claims description 20
- 150000001412 amines Chemical class 0.000 claims description 19
- 230000008929 regeneration Effects 0.000 claims description 18
- 238000011069 regeneration method Methods 0.000 claims description 18
- 239000012492 regenerant Substances 0.000 claims description 17
- GNFTZDOKVXKIBK-UHFFFAOYSA-N 3-(2-methoxyethoxy)benzohydrazide Chemical compound COCCOC1=CC=CC(C(=O)NN)=C1 GNFTZDOKVXKIBK-UHFFFAOYSA-N 0.000 claims description 10
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 claims description 10
- YTAHJIFKAKIKAV-XNMGPUDCSA-N [(1R)-3-morpholin-4-yl-1-phenylpropyl] N-[(3S)-2-oxo-5-phenyl-1,3-dihydro-1,4-benzodiazepin-3-yl]carbamate Chemical compound O=C1[C@H](N=C(C2=C(N1)C=CC=C2)C1=CC=CC=C1)NC(O[C@H](CCN1CCOCC1)C1=CC=CC=C1)=O YTAHJIFKAKIKAV-XNMGPUDCSA-N 0.000 claims description 10
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 claims description 10
- 229940043276 diisopropanolamine Drugs 0.000 claims description 10
- 238000000746 purification Methods 0.000 claims description 7
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical group NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 claims description 5
- 239000000654 additive Substances 0.000 claims description 5
- 230000000996 additive effect Effects 0.000 claims description 5
- 239000007864 aqueous solution Substances 0.000 claims description 5
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 claims description 5
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 abstract description 6
- 238000011084 recovery Methods 0.000 abstract 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 25
- 239000011347 resin Substances 0.000 description 12
- 229920005989 resin Polymers 0.000 description 12
- 239000003513 alkali Substances 0.000 description 8
- 230000002829 reductive effect Effects 0.000 description 8
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 239000010865 sewage Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 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 3
- -1 alcohol amine Chemical class 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 238000003912 environmental pollution Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000003456 ion exchange resin Substances 0.000 description 3
- 229920003303 ion-exchange polymer Polymers 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 230000036961 partial effect Effects 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000008234 soft water Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 229910001413 alkali metal ion Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 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 1
- 230000003628 erosive effect Effects 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 235000019600 saltiness Nutrition 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Abstract
The invention relates to a method for reducing dosage and discharge of flushing liquor for a device of removing heat stable salts in a solvent. The method comprises the following steps: a, allowing unpurified solvent to pass through a filter to eject residual flushing liquor to be recycled to a recovery tank; b, returning the purified solvent back to a user system; c, pressing the flushing liquor out by using purifying air to carry out back flushing, and leading the flushing liquor to enter a solvent system; d, utilizing the external flushing liquor to carry out deep flushing, and leading the flushing liquor to enter the solvent system; e, enabling the flushing liquor to enter into the recovery tank; f, pressing reclaiming agent solution out by using the external flushing liquor and the purifying air to the recovery tank; g, pressing the reclaiming agent solution out by using the purifying air and discharging waste reclaiming agent solution; h, pressing the flushing liquor out by using the purifying air, wherein the flushing liquor is not discharged outwards; i, continuously pressing the flushing liquor out by using the purifying air in the recovery tank, flushing, discharging outwards; j, carrying out deep flushing with the external flushing liquor; k, enabling the exterior flushing liquor to flow to the recovery tank; and l, introducing external reclaiming agent solution to the recover tank, wherein the steps i and l are synchronously carried out. The invention is environment-friendly and reduces cost.
Description
Technical field
The present invention relates to the method that a kind of minimizing removes heat stable salts device washing fluid consumption and discharging in the solvent.
Background technology
China's sulphur-bearing crude and high-sulfur crude oil amount of finish constantly increase, and the respective environment law is strict day by day, has promoted the development of desulfurization technology and the renewal of desulfurization solvent.For Sweet natural gas and refinery gas purification, the desulfurization of hydramine method is in dominant position so far, is considered to the most effective technology.Operation along with amine liquid desulfurizer, because of degrading solvent, impurity, erosion resistant agent and foam inhibiting agent such as bring at reason in the unstripped gas, heat stable salts constantly generates and accumulation in solvent systems, make partial solvent in bond and can not obtain regeneration, have influence on the desulfuration efficiency of device, fluctuation of service, and hydrogen sulfide situation not up to standard.
The existence of heat stable salts combines with solvent, can not be reproduced in regenerator column, cause the solvent desulfuration efficiency to reduce, increase solvent-oil ratio, and can aggravate corrosion of equipment, promote disadvantageous effects such as solvent foaming, remove a kind of effective ways that heat stable salts is proved to be to address this problem in the solvent.
The AmiPur device that for example Canadian Eco-Tec company produces comes into operation in Zhenghai refinery company catalysis workshop of oil refining in August, 2003, adopts the method for anionite-exchange resin to remove heat stable salts negatively charged ion in the poor amine liquid.The process of system's whole service is: do not purify amine liquid through filter, enter heat stable salts and remove the unit, purify back amine liquid and be back to custom system.Afterwards with the residual amine liquid of de-mineralized water flushing resin bed.Then sodium hydroxide solution enters resin bed, and resin is regenerated, and regeneration waste liquid is discharged at the bottom of bed, is again that de-mineralized water is towards the residual alkali lye of resin bed then.Regenerating to resin with sodium hydroxide in the saturated back of resin, needs after the regeneration resin bed is washed, and this just needs the regenerative wastewater and the flushing waste water of discharging sodium hydroxide.According to on-the-spot running condition, under the normal circumstances, 3 cycles of operation each hour, about 70 liters of the loadings of ion exchange resin, the about 260L waste lye of each cycle discharging, every day, waste liquid amount reached 18.7 tons, had brought very big pressure to sewage disposal aspect environmental protection.[Lin Xiaohong, Yuan Zhangyong. with the thermal-stable salt [J] in the AmiPur amine purification techniques removal amine method desulfurizer amine liquid. refining of petroleum and chemical industry, 2004,35 (8): 22-25]
For example the HSSX of U.S. MPR company production is installed on and comes into operation at Chongqing natural gas conditioning head factory in August, 2005, adopts the method for ion-exchange that the heat stable salts in the amine liquid is removed.Whole device technique is formed one-period by desalination, cleaning, regeneration, four steps of cleaning.The first step utilizes ion exchange resin to remove heat stable salts, ion exchange resin reach saturated after, get back in the system with residual amine liquid in the soft water flushing resin; Alkali lye with 5% is regenerated to resin, after regeneration finishes, has a large amount of alkali lye in the resin, and this part alkali lye can not be brought in the system, need wash with soft water, and sewage discharge begins second period then, one day 3-8 cycle.During resin regeneration, alkali lye discharge water and alkali lye wash-down water are main sewage sources, and how much relevant the size of amount is with the solution saltiness, approximately handles 1m
3This device of amine liquid produces 1.5～2.4m
3About sewage, the sewage generation is bigger.[Chen Hui, Wan Yixiu, He Ming etc. ion exchange technique removes the applied analysis [J] of thermo-stabilising salts in the amine liquid. oil and gas chemical industry, 200633 (4): 298-299].
The processing that contains alkali waste water is the hard nut to crack of petrochemical industry always, has been listed in the public relations project of group of China Petrochemical Industry environmental protection.Therefore, fail to obtain fully reasonably under the disposal situation containing alkali waste water, the quantity discharged that reduces waste lye as much as possible is to remove the problem that heat stable salts system in the solvent needs solution badly.
Summary of the invention
The present invention is directed to that to remove in the solvent discharging of heat stable salts system regeneration flushing waste in the prior art excessive, the shortcoming that environmental pollution is big, a kind of reuse partial flushing liquid is provided, reduce the consumption and the discharging waste liquid of wash-down water, environment amenable minimizing removes the method for heat stable salts device washing fluid consumption and discharging in the solvent.
In order to solve the problems of the technologies described above, the present invention is solved by following technical proposals:
Reduce the method remove heat stable salts device washing fluid consumption and discharging in the solvent, comprise the following steps:
Step a: purifying solvent does not enter heat stable salts and removes the unit through filter, ejects residuing in the washing fluid that heat stable salts removes in the unit, and reuse is to withdrawing can;
Step b: the solvent after the purification returns custom system;
Step c: purify wind washing fluid is extruded from withdrawing can, enter heat stable salts and remove the unit, exchang medium is carried out counterflush, washing fluid enters solvent systems;
Steps d: the extraneous washing fluid that inserts, heat stable salts is removed the unit carry out degree of depth flushing, washing fluid enters solvent systems;
Step e: washing fluid is recycled to withdrawing can;
Step f: extraneous insert washing fluid and purify wind the regenerant solution in the withdrawing can is extruded, will residue in heat stable salts and remove unitary washing fluid and extrude to withdrawing can;
Step g: purify wind regenerant solution is further extruded, remove the unit by heat stable salts, regeneration waste liquid removes unitary bottom from this heat stable salts and discharges;
Step h: purify wind the washing fluid of collecting in the withdrawing can is extruded, remove the unit, be recycled to withdrawing can, do not efflux flushing waste through heat stable salts;
Step I: purify wind and continue washing fluid in the withdrawing can is extruded, heat stable salts is removed the unit wash, flushing waste effluxes;
Step j: the extraneous washing fluid that inserts, the heat stable salts of degree of depth flushing from the bottom to top removes the unit;
Step k: the extraneous washing fluid heat stable salts of flowing through removes the unit to withdrawing can;
Step l: the extraneous regenerant solution that inserts enters withdrawing can;
Described step I and step l carry out simultaneously.
As preferably, described withdrawing can is provided with fluid level controller, and step a is controlled by fluid level controller.
As preferably, described withdrawing can is provided with fluid level controller, and step c and step e control by fluid level controller.
As preferably, described heat stable salts removes the unit and is provided with flow director, and steps d and step j control by flow director.
As preferably, described withdrawing can is provided with fluid level controller, and step f, step g and step h control by fluid level controller.
As preferably, described withdrawing can is provided with fluid level controller, and step a, step I and step k control by fluid level controller.
As preferably, described withdrawing can is provided with flow director and pump, and step l is by flow director and pump measure control.
As preferably, described not purifying solvent is pure amine solvent.
As preferably, described pure amine solvent is Monoethanolamine MEA BASF, diethanolamine, diisopropanolamine (DIPA), methyldiethanolamine and the aqueous solution that is added with the complex solvent of additive accordingly.
Remove three washing fluid withdrawing cans of increase and control corresponding unit on the unitary basis at existing heat stable salts.Regenerator removes the unit by heat stable salts, and the exchang medium that loads in this unit is regenerated.Behind this end of processing, brought into the performance that solvent systems has a negative impact and keeps exchang medium because of the alkalimetal ion of regenerator, need be carried out wash-out to the regenerator that residues in exchang medium with enough washing fluids for reducing; Purifying solvent does not carry out removing of heat stable salts through exchang medium, needs the washing fluid of capacity that the solvent that residues in exchang medium is carried out wash-out, is loss in order to avoid cause solvent.
The principle of design of withdrawing can is a control mode of utilizing liquid level and flow to combine, the dope of the initial stage of a certain amount of regeneration flushing is collected into withdrawing can is used for next round-robin regenerative process; Secondly, the clear liquid of the later stage of a certain amount of regeneration flushing is collected be recycled to withdrawing can and be used for next round-robin regeneration flushing process; Once more, will the washing fluid that remove behind the heat stable salts be reclaimed, be used for next cycle to desalination after the flushing of exchang medium.
The present invention has significant technique effect owing to adopted above technical scheme:
The inventive method will remove the flushing of heat stable salts unit to identical clean degree, the consumption of 30%-50% washing fluid has been saved in the design of three withdrawing cans, reduced the quantity discharged of about 38%-45% regeneration waste liquid, environmentally friendly, effectively reduce environmental pollution improvement's cost.
Description of drawings
Fig. 1 is a schematic flow sheet of the present invention.
The toponym that each number designation referred in the above accompanying drawing is as follows: wherein 1-withdrawing can, 2-withdrawing can, 3-withdrawing can, 4-heat stable salts remove unit, 5-strainer, 6-fluid level controller, 7-fluid level controller, 8-fluid level controller, 9-flow director, 10-flow director, 11-pump.
Embodiment
Below in conjunction with accompanying drawing 1 and specific embodiment the present invention is described in further detail:
Embodiment 1
Reduce the method remove heat stable salts device washing fluid consumption and discharging in the solvent, as shown in Figure 1, comprise the following steps:
Step a: purifying solvent does not enter heat stable salts and removes unit 4 through filter 5, ejects residuing in the washing fluids that heat stable salts removes in the unit 4, and reuse is to withdrawing can 2;
Step b: the solvent after the purification returns custom system;
Step c: purify wind washing fluid is extruded from withdrawing can 3, enter heat stable salts and remove unit 4, exchang medium is carried out counterflush, washing fluid enters solvent systems;
Steps d: the extraneous washing fluid that inserts, heat stable salts is removed unit 4 carry out degree of depth flushing, washing fluid enters solvent systems;
Step e: washing fluid is recycled to withdrawing can 3;
Step f: extraneous insert washing fluid and purify wind the regenerant solution in the withdrawing can 1 is extruded, extrude to withdrawing can 2 residuing in the washing fluid that heat stable salts removes unit 4;
Step g: purify wind regenerant solution is further extruded, remove unit 4 by heat stable salts, regeneration waste liquid is discharged from the bottom that this heat stable salts removes unit 4;
Step h: purify wind the washing fluid of collecting in the withdrawing can 2 is extruded, remove unit 4, be recycled to withdrawing can 1, do not efflux flushing waste through heat stable salts;
Step I: purify wind and continue washing fluid in the withdrawing can 2 is extruded, heat stable salts is removed unit 4 wash, flushing waste effluxes;
Step j: the extraneous washing fluid that inserts, the heat stable salts of degree of depth flushing from the bottom to top removes unit 4;
Step k: the extraneous washing fluid heat stable salts of flowing through removes unit 4 to withdrawing can 2;
Step l: the extraneous regenerant solution that inserts enters withdrawing can 1;
Described step I and step l carry out simultaneously.
Withdrawing can 2 is provided with fluid level controller 7, and step a is by fluid level controller 7 controls.
Withdrawing can 3 is provided with fluid level controller 8, and step c and step e are by fluid level controller 8 controls.
Heat stable salts removes unit 4 and is provided with flow director 9, and steps d and step j are by flow director 9 controls.
Withdrawing can 1 is provided with fluid level controller 6, and step f, step g and step h are by fluid level controller 6 controls.
Withdrawing can 2 is provided with fluid level controller 7, and step a, step I and step k are by fluid level controller 7 controls.
Withdrawing can 1 is provided with flow director 10 and pump 11, and step l is by flow director 10 and pump 11 measure control.
Purifying solvent is not pure amine solvent.
The alcohol amine solvent is Monoethanolamine MEA BASF, diethanolamine, diisopropanolamine (DIPA), methyldiethanolamine and the aqueous solution that is added with the complex solvent of additive accordingly.
When purifying solvent not with 3500 liters of flows/time, through strainer 5, the heat stable salts that enters volume and be 70 liters removes unit 4.125 liters of the volumes of withdrawing can 1 are set, and the volume of withdrawing can 2 is 135 liters, and the volume of withdrawing can 3 is 150 liters.In each circulation, withdrawing can 1 reuse 100 liters, withdrawing can 2 altogether reuses 120 liters, withdrawing can 3 reuses 140 liters.Reach under the identical clean level at the flushing exchang medium, before the design that increases withdrawing can, the consumption of washing fluid has reduced 48.9%, and the flushing waste discharging has reduced 38.2%.
Embodiment 2
Reduce the method remove heat stable salts device washing fluid consumption and discharging in the solvent, as shown in Figure 1, comprise the following steps:
Step a: purifying solvent does not enter heat stable salts and removes unit 4 through filter 5, ejects residuing in the washing fluids that heat stable salts removes in the unit 4, and reuse is to withdrawing can 2;
Step b: the solvent after the purification returns custom system;
Step c: purify wind washing fluid is extruded from withdrawing can 3, enter heat stable salts and remove unit 4, exchang medium is carried out counterflush, washing fluid enters solvent systems;
Steps d: the extraneous washing fluid that inserts, heat stable salts is removed unit 4 carry out degree of depth flushing, washing fluid enters solvent systems;
Step e: washing fluid is recycled to withdrawing can 3;
Step f: extraneous insert washing fluid and purify wind the regenerant solution in the withdrawing can 1 is extruded, extrude to withdrawing can 2 residuing in the washing fluid that heat stable salts removes unit 4;
Step g: purify wind regenerant solution is further extruded, remove unit 4 by heat stable salts, regeneration waste liquid is discharged from the bottom that this heat stable salts removes unit 4;
Step h: purify wind the washing fluid of collecting in the withdrawing can 2 is extruded, remove unit 4, be recycled to withdrawing can 1, do not efflux flushing waste through heat stable salts;
Step I: purify wind and continue washing fluid in the withdrawing can 2 is extruded, heat stable salts is removed unit 4 wash, flushing waste effluxes;
Step j: the extraneous washing fluid that inserts, the heat stable salts of degree of depth flushing from the bottom to top removes unit 4;
Step k: the extraneous washing fluid heat stable salts of flowing through removes unit 4 to withdrawing can 2;
Step l: the extraneous regenerant solution that inserts enters withdrawing can 1;
Described step I and step l carry out simultaneously.
Withdrawing can 2 is provided with fluid level controller 7, and step a is by fluid level controller 7 controls.
Withdrawing can 3 is provided with fluid level controller 8, and step c and step e are by fluid level controller 8 controls.
Heat stable salts removes unit 4 and is provided with flow director 9, and steps d and step j are by flow director 9 controls.
Withdrawing can 1 is provided with fluid level controller 6, and step f, step g and step h are by fluid level controller 6 controls.
Withdrawing can 2 is provided with fluid level controller 7, and step a, step I and step k are by fluid level controller 7 controls.
Withdrawing can 1 is provided with flow director 10 and pump 11, and step l is by flow director 10 and pump 11 measure control.
Purifying solvent is not pure amine solvent.
The alcohol amine solvent is Monoethanolamine MEA BASF, diethanolamine, diisopropanolamine (DIPA), methyldiethanolamine and the aqueous solution that is added with the complex solvent of additive accordingly.
When purifying solvent not with 2500 liters of flows/time, through strainer 5, the heat stable salts that enters volume and be 25 liters removes unit 4.40 liters of the volumes of withdrawing can 1 are set, and the volume of withdrawing can 2 is 50 liters, and the volume of withdrawing can 3 is 60 liters.In each circulation, withdrawing can 1 reuse 35.5 liters, withdrawing can 2 altogether reuses 45 liters, withdrawing can 3 reuses 50 liters.Reach under the identical clean level at the flushing exchang medium, before the design that increases withdrawing can, the consumption of washing fluid has reduced 49%, and the flushing waste discharging has reduced 42.5%.
Embodiment 3
Reduce the method remove heat stable salts device washing fluid consumption and discharging in the solvent, as shown in Figure 1, comprise the following steps:
Step a: purifying solvent does not enter heat stable salts and removes unit 4 through filter 5, ejects residuing in the washing fluids that heat stable salts removes in the unit 4, and reuse is to withdrawing can 2;
Step b: the solvent after the purification returns custom system;
Step c: purify wind washing fluid is extruded from withdrawing can 3, enter heat stable salts and remove unit 4, exchang medium is carried out counterflush, washing fluid enters solvent systems;
Steps d: the extraneous washing fluid that inserts, heat stable salts is removed unit 4 carry out degree of depth flushing, washing fluid enters solvent systems;
Step e: washing fluid is recycled to withdrawing can 3;
Step f: extraneous insert washing fluid and purify wind the regenerant solution in the withdrawing can 1 is extruded, extrude to withdrawing can 2 residuing in the washing fluid that heat stable salts removes unit 4;
Step g: purify wind regenerant solution is further extruded, remove unit 4 by heat stable salts, regeneration waste liquid is discharged from the bottom that this heat stable salts removes unit 4;
Step h: purify wind the washing fluid of collecting in the withdrawing can 2 is extruded, remove unit 4, be recycled to withdrawing can 1, do not efflux flushing waste through heat stable salts;
Step I: purify wind and continue washing fluid in the withdrawing can 2 is extruded, heat stable salts is removed unit 4 wash, flushing waste effluxes;
Step j: the extraneous washing fluid that inserts, the heat stable salts of degree of depth flushing from the bottom to top removes unit 4;
Step k: the extraneous washing fluid heat stable salts of flowing through removes unit 4 to withdrawing can 2;
Step l: the extraneous regenerant solution that inserts enters withdrawing can 1;
Described step I and step l carry out simultaneously.
Withdrawing can 2 is provided with fluid level controller 7, and step a is by fluid level controller 7 controls.
Withdrawing can 3 is provided with fluid level controller 8, and step c and step e are by fluid level controller 8 controls.
Heat stable salts removes unit 4 and is provided with flow director 9, and steps d and step j are by flow director 9 controls.
Withdrawing can 1 is provided with fluid level controller 6, and step f, step g and step h are by fluid level controller 6 controls.
Withdrawing can 2 is provided with fluid level controller 7, and step a, step I and step k are by fluid level controller 7 controls.
Withdrawing can 1 is provided with flow director 10 and pump 11, and step l is by flow director 10 and pump 11 measure control.
Purifying solvent is not pure amine solvent.
The alcohol amine solvent is Monoethanolamine MEA BASF, diethanolamine, diisopropanolamine (DIPA), methyldiethanolamine and the aqueous solution that is added with the complex solvent of additive accordingly.
When purifying solvent not with 1000 liters of flows/time, through strainer 5, the heat stable salts that enters volume and be 10 liters removes unit 4.15 liters of the volumes of withdrawing can 1 are set, and the volume of withdrawing can 2 is 20 liters, and the volume of withdrawing can 3 is 25 liters.In each circulation, withdrawing can 1 reuse 13 liters, withdrawing can 2 altogether reuses 16 liters, withdrawing can 3 reuses 20 liters.Reach under the identical clean level at the flushing exchang medium, before the design that increases withdrawing can, the consumption of washing fluid has reduced 30.7%, and the flushing waste discharging has reduced 40%.
Desuperheating stable salts system increases withdrawing can front and back supplies consumption and discharging synopsis
In each working cycle of above-mentioned three embodiment, withdrawing can 2 reuses not purifying solvent remove the washing fluid that unit 4 ejects at first through heat stable salts only, withdrawing can 2 also reuse regenerant solution enter heat stable salts and remove the unit 4 initial washing fluids that extrude.The washing fluid of this two portions reuse is recycled to withdrawing can 1 again with doing that heat stable salts is removed flushing after unit 4 regeneration, is used for the configuration of regenerant solution.Withdrawing can 3 has reclaimed after purifying solvent does not remove heat stable salts, and washing fluid is to this unitary washing fluid of washing the later stage, and as required washing fluid in this step flushing early stage.Saved the consumption of washing fluid like this, the quantity discharged of flushing waste (clear liquid).Whole process, by liquid level control, flow control and corresponding valve combination form automatic control.
The inventive method will remove the flushing of heat stable salts unit to identical clean degree, the consumption of 30%-50% washing fluid has been saved in the design of three withdrawing cans, reduced the quantity discharged of about 38%-45% regeneration waste liquid, environmentally friendly, effectively reduce environmental pollution improvement's cost.
In a word, the above only is preferred embodiment of the present invention, and all equalizations of being done according to the present patent application claim change and modify, and all should belong to the covering scope of patent of the present invention.
Claims (9)
1. reduce the method remove heat stable salts device washing fluid consumption and discharging in the solvent, it is characterized in that: comprise the following steps:
Step a: purifying solvent does not enter heat stable salts and removes unit (4) through filter (5), will residue in the washing fluid that heat stable salts removes in the unit (4) and eject, and reuse is to withdrawing can (2);
Step b: the solvent after the purification returns custom system;
Step c: purify wind washing fluid is extruded from withdrawing can (3), enter heat stable salts and remove unit (4), exchang medium is carried out counterflush, washing fluid enters solvent systems;
Steps d: the extraneous washing fluid that inserts, heat stable salts is removed unit (4) carry out degree of depth flushing, washing fluid enters solvent systems;
Step e: washing fluid is recycled to withdrawing can (3);
Step f: extraneous insert washing fluid and purify wind the regenerant solution in the withdrawing can (1) is extruded, will residue in the washing fluid that heat stable salts removes unit (4) and extrude to withdrawing can (2);
Step g: purify wind regenerant solution is further extruded, remove unit (4) by heat stable salts, regeneration waste liquid is discharged from the bottom that this heat stable salts removes unit (4);
Step h: purify wind the washing fluid of collecting in the withdrawing can (2) is extruded, remove unit (4), be recycled to withdrawing can (1), do not efflux flushing waste through heat stable salts;
Step I: purify wind and continue washing fluid in the withdrawing can (2) is extruded, heat stable salts is removed unit (4) wash, flushing waste effluxes;
Step j: the extraneous washing fluid that inserts, the heat stable salts of degree of depth flushing from the bottom to top removes unit (4);
Step k: the extraneous washing fluid heat stable salts of flowing through removes unit (4) to withdrawing can (2);
Step l: the extraneous regenerant solution that inserts enters withdrawing can (1);
Described step I and step l carry out simultaneously.
2. minimizing according to claim 1 removes the device of heat stable salts device washing fluid consumption and discharging in the solvent, and it is characterized in that: described withdrawing can (2) is provided with fluid level controller (7), and step a is controlled by fluid level controller (7).
3. minimizing according to claim 1 removes the method for heat stable salts device washing fluid consumption and discharging in the solvent, and it is characterized in that: described withdrawing can (3) is provided with fluid level controller (8), and step c and step e control by fluid level controller (8).
4. minimizing according to claim 1 removes the method for heat stable salts device washing fluid consumption and discharging in the solvent, it is characterized in that: described heat stable salts removes unit (4) and is provided with flow director (9), and steps d and step j control by flow director (9).
5. minimizing according to claim 1 removes the method for heat stable salts device washing fluid consumption and discharging in the solvent, it is characterized in that: described withdrawing can (1) is provided with fluid level controller (6), and step f, step g and step h control by fluid level controller (6).
6. minimizing according to claim 1 removes the method for heat stable salts device washing fluid consumption and discharging in the solvent, it is characterized in that: described withdrawing can (2) is provided with fluid level controller (7), and step a, step I and step k control by fluid level controller (7).
7. minimizing according to claim 1 removes the method for heat stable salts device washing fluid consumption and discharging in the solvent, it is characterized in that: described withdrawing can (1) is provided with flow director (10) and pump (11), and step l is by flow director (10) and pump (11) measure control.
8. minimizing according to claim 1 removes the method for heat stable salts device washing fluid consumption and discharging in the solvent, and it is characterized in that: described not purifying solvent is pure amine solvent.
9. minimizing according to claim 8 removes the method for heat stable salts device washing fluid consumption and discharging in the solvent, it is characterized in that: described pure amine solvent is Monoethanolamine MEA BASF, diethanolamine, diisopropanolamine (DIPA), methyldiethanolamine and the aqueous solution that is added with the complex solvent of additive accordingly.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6106722A (en) * | 1997-08-12 | 2000-08-22 | Kinetico Incorporated | Filtering photoresist-containing liquid |
| WO2007057012A1 (en) * | 2005-11-17 | 2007-05-24 | Danfoss A/S | Liquid treatment arrangement, in particular water treatment arrangement |
| CN101219815A (en) * | 2008-01-29 | 2008-07-16 | 王建军 | Cleaning treatment system |
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2010
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6106722A (en) * | 1997-08-12 | 2000-08-22 | Kinetico Incorporated | Filtering photoresist-containing liquid |
| WO2007057012A1 (en) * | 2005-11-17 | 2007-05-24 | Danfoss A/S | Liquid treatment arrangement, in particular water treatment arrangement |
| CN101219815A (en) * | 2008-01-29 | 2008-07-16 | 王建军 | Cleaning treatment system |
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