CN100333823C - Method for purifying deterioration amine liquid using highly basic anion exchange resin - Google Patents

Method for purifying deterioration amine liquid using highly basic anion exchange resin Download PDF

Info

Publication number
CN100333823C
CN100333823C CNB2004100534700A CN200410053470A CN100333823C CN 100333823 C CN100333823 C CN 100333823C CN B2004100534700 A CNB2004100534700 A CN B2004100534700A CN 200410053470 A CN200410053470 A CN 200410053470A CN 100333823 C CN100333823 C CN 100333823C
Authority
CN
China
Prior art keywords
resin
amine liquid
deterioration
exchange resin
amine
Prior art date
Application number
CNB2004100534700A
Other languages
Chinese (zh)
Other versions
CN1733355A (en
Inventor
罗芳
曹全胜
李天金
马竞涛
聂通元
Original Assignee
中国石化镇海炼油化工股份有限公司
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 中国石化镇海炼油化工股份有限公司 filed Critical 中国石化镇海炼油化工股份有限公司
Priority to CNB2004100534700A priority Critical patent/CN100333823C/en
Publication of CN1733355A publication Critical patent/CN1733355A/en
Application granted granted Critical
Publication of CN100333823C publication Critical patent/CN100333823C/en

Links

Abstract

The present invention discloses a method for purifying deterioration amine liquid by highly basic anion exchange resin, which uses heat steady-state salt in deterioration alcohol amine solution in desulfurizing devices, etc. according to an amine eliminating method by the highly basic anion exchange resin, and the method for purifying deterioration amine liquid by highly basic anion exchange resin carries out the regeneration of the resin by the use of a sodium hydroxide one-step method and the periodic use of a sodium chloride anabiotic technology. The adopted highly basic anion exchange resin can be 1 type phenylethylene-divinylbenzene framework highly basic anion exchange resin, 2 type phenylethylene-divinylbenzene framework highly basic anion exchange resin and acrylic acid framework highly basic anion exchange resin. The method for purifying deterioration amine liquid by highly basic anion exchange resin has the advantages that the resin has the strong capability of eliminating and absorbing sulfur hydrogen acid radicals, and the resin can be used for eliminating the heat steady-state salt in the amine liquid in a long period; the technology of the resin regeneration is easy, the purification efficiency of the amine liquid is high, and the exchange capacity of the resin can be kept to about 77%.

Description

A kind of method that purifies deterioration amine liquid with strong-base anion-exchange resin
Technical field
The present invention relates to the ion-exchange purification techniques, is the method that a kind of spent ion exchange resin is removed the impurity such as heat stable salts in the deterioration amine liquid specifically.
Background technology
Natural gas plant and oil plant are usually with the H in the hydramine absorption plant removal air-flow (natural gas, dry gas, liquefied gas and the petroleum gas that comes self-catalysis, cracking, coking etc. to install) 2S and CO 2Sour gas, absorbent mainly are 20%~50% aqueous alkanolamines." the amine liquid " of indication of the present invention is general name, various alkanolamines (one or more) aqueous solution that is considered when comprising desulfurization and adopts, as: MEA (MEA), diethanol amine (DEA), triethanolamine (TEA), diglycolamine (DGA), diisopropanolamine (DIPA) and methyl diethanolamine (MDEA).
The technical process of acid gas removal body is to make air communication cross the amine absorption tower, with poor amine liquid counter current contacting, CO 2And H 2The S sour gas is dissolved in the amine liquid, and to form soluble pure amine salt (be protonated hydramine cation and HS-and HCO 3-In conjunction with).Then, water, unreacted hydramine and pure amine salt solution enter stripper, and this class hydramine salinity is separated and discharged H 2S and CO 2, amine liquid circulates once more and enters absorption tower and stripper.But, remove H in the air-flow 2S and CO 2Also comprise SO outward, 2, CS 2, sour gas such as HCN and COS, these gases carry out and the reaction of amine liquid, form alkanolamine equally.And these salt can not be removed by stripper, are trapped in the system and constantly accumulation.
Another problem is, if oxygen enters the alkanolamine system, sour gas and hydramine oxidation form other pure amine salt, and modal is thiosulfuric acid (S 2O 3 2-) salt, sulfuric acid (SO 4 2-) salt, thiocyanic acid (SCN -) salt, polythionate, acetate, formates, nitrate and chlorine (Cl -) salt etc., these salt can not be regenerated by stripper.
Can not be referred to as heat stable salts (Heat Stable Salts is called for short HSS) by the pure amine salt of heat regeneration, it brings following harm to device: one of major reason of equipment heavy corrosion; Salt and corrosion product cause the obstruction of device; The heat stable salts anion combines with amine and forms constraint amine, has reduced effective amine concentration of amine liquid, makes the desulfuration efficiency of amine liquid descend; The heat stable salts of high-load also makes the foaming trend aggravation of amine liquid, further reduces the device desulfuration efficiency and makes the amine liquid of device run the consumption increase.Thereby need it is handled.
How to solve the heat stable salts problem in the amine liquid, domestic still do not have processing method preferably at present, mainly is that amine liquid is emitted or disposes, and normally regularly emits a part of amine.Because the COD content higher (6% amine liquid COD mass concentration reaches 30, more than the 000mg/L) of amine liquid is bigger to the sewage disposal system impact if enter sewage, and environment and human body are constituted harm.Another kind method is that dirty amine liquid is introduced delayed coking unit, carry out pyrolytic and handle (with reference to " petroleum refining and chemical industry " the 34th volume the 1st phase " delayed coking unit processing disused aine liquid "), but this technology causes problems such as corrosion of heating furnace water injection pipe and the obstruction of coking fractional distillation column tower tray easily.
Similar techniques is disclosed Chinese patent CN1 on October 6th, 1999,230, and the disclosed a kind of method of 545A with anion exchange resin regeneration inferior sulfolane.This method is earlier through distillation, again by macroreticular weakly base styrene anion exchange resin layer, to remove acidic materials wherein with inferior sulfolane.
Purify amine liquid and be to use the way of distillation the earliest.The way of distillation can be applied to the MEA system, but can not in diethanol amine (DEA), triethanolamine (TEA) and methyl diethanolamine systems such as (MDEA), use, because the boiling point of these alkanolamines is very high (under the 760mmHg,>400F), oxidation and degraded take place in hydramine easily under so high temperature.And prevent that the amine thermal degradation from must use decompression distillation, but that decompression distillation purifies the equipment and the operating cost of amine liquid is too high, so the way of distillation never is applied to remove the heat stable salts in the amine liquid.
Spent ion exchange resin is removed the method for the heat stable salts in the amine liquid and is compared with other amine liquid purification methods, has low, the simple characteristics of expense.But owing to not only contain heat stable salts in the deterioration amine liquid but also contain the hydramine degradable component of chemical composition complexity, as " HEED ", " BHEEU " etc. contains organic impurities in addition in the amine liquid, pollute resin easily, increased difficulty for ion-exchange purification amine liquid.Water treatment facilities uses ion exchange technique very successful, but the anion total concentration in the water is much lower, and the ion that has strong affinity with resin still less, so the regeneration of ion-exchange resin ratio is easier to, and is also lower to the requirement of resin.On the contrary, the anion concentration of amine treatment system is very high, needs frequent regeneration to remove these anion.In addition, the anion stronger with resin affinity is as sulfur hydrogen anion, formate, acetate etc., because of being difficult to desorption from the cation adsorption group of resin.So use ion-exchange purification regeneration deterioration amine liquid, most critical be to select the type of resin and the technology of resin regeneration for use.
In U.S. Patent No. 5, in 162,084, use sulfuric acid and NaOH regenerating resin, I type styrene-divinylbenzene skeleton strong-base anion-exchange resin is selected in special recommendation for use, because I type resin exchange capacity is than II type styrene-divinylbenzene skeleton strong-base anion-exchange resin height.
In U.S. Patent No. 5,788, in 864, adopt the regeneration of NaOH one-step method, it selects highly basic II type styrene-divinylbenzene skeleton strong-base anion-exchange resin for use, and the exchange capacity of regeneration back resin can return to original about 50%.
Summary of the invention
Technical problem to be solved by this invention is that a kind of method that purifies deterioration amine liquid with strong-base anion-exchange resin is provided at the prior art present situation, this method can apply to the purified treatment of deterioration amine liquid in the device such as amine method desulfurization and the regeneration of exchanger resin, to remove impurity such as heat stable salts anion in the amine liquid and amine liquid is used for recirculation, guarantee that amine aqueous solution moves under low heat stable salts content.
The present invention solves the problems of the technologies described above the technical scheme that is adopted: this kind purifies the method for deterioration amine liquid with strong-base anion-exchange resin, it is characterized in that may further comprise the steps:
A, absorption: with temperature is that 30~60 ℃ and the deterioration amine liquid handled are after filtration flowed through and are filled with the resin bed of strong-base anion-exchange resin, and the heat stable salts anion in the resin adsorption deterioration amine liquid is purified deterioration amine liquid; When purifying amine liquid because of the employing suction type, the anion load in the resin bed constantly increases, so need remove the anion that adsorbs in the resin bed by following step b;
B, regeneration: after treating that resin adsorption in the described resin bed is saturated, wash described resin bed, make the resin in the described resin bed obtain regeneration and recover adsorption capacity substantially with alkali metal hydroxide aqueous solution;
C, repetition above-mentioned steps a and step b;
D, recovery: whenever carry out above-mentioned steps a and step b the circulation 50~200 times after, wash described resin bed with sodium-chloride water solution, remove the organic matter and the stronger SCN of affinity that are adsorbed on the resin -, to keep the ion exchange capacity of resin; It should be noted that and then can reduce amine liquid purification efficiency, and the concentration of chlorion in the amine liquid is increased, so the present invention adopts the method that regularly makes the resin recovery with the sodium-chloride water solution flushing if sodium-chloride water solution is used in resin regeneration at every turn.
Described strong-base anion-exchange resin can be selected I type styrene-divinylbenzene skeleton strong-base anion-exchange resin (hereinafter to be referred as I type styrene resin), II type styrene-divinylbenzene skeleton strong-base anion-exchange resin (hereinafter to be referred as II type styrene resin) or acrylic backbone strong-base anion-exchange resin (hereinafter to be referred as acrylic resin) for use.
Filtration in the described adsorption step comprises multistage filtering, wherein should comprise with active carbon filter at least and filtering.
Whether the method that the present invention purifies deterioration amine liquid also comprises the heat stable salts analysis on Content in the gained amine liquid after described adsorption treatment, to determine the time that the ion exchange resin adion reaches capacity and to need the resin processing of regenerating.
If the single resin bed of purification of deterioration amine liquid of the present invention, technology is step, because need stop into amine liquid when ion exchange resin regeneration.If use plural a plurality of resin bed parallel connection, handover operation between the resin bed in parallel then can be realized carrying out continuously of deterioration amine liquid purification.
Described alkali metal hydroxide aqueous solution preferably concentration is the sodium hydrate aqueous solution of 10~20wt%.
The concentration of described sodium-chloride water solution is preferably 1~20wt%.
Described deterioration amine liquid refers to that the content of heat stable salts wherein is the aqueous solution of one or more hydramine of 1~15%, and hydramine comprises MEA, diethanol amine, triethanolamine, diglycolamine, diisopropanolamine (DIPA) and methyl diethanolamine etc.
Described heat stable salts anion comprises organic acid, sour gas and inorganic acid radical.Described organic acid comprises HCOO -, CH 3COO -And oxalate etc.; Described inorganic acid radical comprises SCN -, Cl -, S 2O 3 2-, SO 4 2-And NO 3 -Deng; Described sour gas comprises SO 2, CS 2, HCN, COS and polythionic acid etc.
Therefore, the inventive method can be summarized as: purify deterioration amine liquid with strong-base anion-exchange resin, the heat stable salts anion in the amine liquid is removed in absorption, make amine liquid be used for recirculation, regeneration of resin then adopts the regeneration of NaOH one-step method and regularly uses the technology of sodium chloride solution recovery.The effect of using sodium chloride solution to recover regularly is to improve the exchange capacity after resin is repeatedly regenerated for a long time.
Utilization the inventive method has following effect:
1. greatly reduce equipment corrosion, prolong the service life of amine treating apparatus, reduce the maintenance and operation expense of equipment.
2. reduce the amine liquid loss of amine treating apparatus, reduced the operating cost of device.
3. improved the desulfuration efficiency (, having increased the amine amount that can be used for handling gas) of desulfurizer, guaranteed the quality of gas treatment equipment product owing to discharge constraint amine.
The inventive method has the following advantages with respect to prior art:
1, adopt strong-base anion-exchange resin to purify amine liquid, the thiocyanate ion that affinity is stronger and other heat stable salts ions are wash-out from resin more easily, and this resin has the strong and not breakable advantage of good springiness of anti-organic matter pollution capacity.Wherein, especially be good with acrylic resin, because adopt acrylic resin to purify amine liquid, the thiocyanate ion that affinity is stronger and other heat stable salts ions are wash-out from resin more easily, and acrylic resin has the strong and not breakable advantage of good springiness of anti-organic matter pollution capacity, and its exchange capacity is also higher in addition.
2, the present invention selects strong-base anion-exchange resin especially for use, is applied to purify amine liquid, removes heat stable salts in the amine liquid.Strong-base anion-exchange resin has the good stronger SCN of desorption affinity -Ability adopts the regeneration of NaOH one-step method, and the exchange capacity of resin can remain on about 65%.
3, the present invention's strong-base anion-exchange resin, continuously purifying heat stable salts content is the amine liquid of 1~15wt%, adopts the repeatedly regeneration for a long time of NaOH one-step method, the exchange capacity of resin can remain on 59%.
4, the present invention's strong-base anion-exchange resin, continuously purifying heat stable salts content is the amine liquid of 1~15wt%, adopt the regeneration of NaOH one-step method, regularly use sodium-chloride water solution flushing recovery again, resin still can remain on 77% through the long-term exchange capacity that uses.This regeneration technology can make resin keep purifying efficiently for a long time amine liquid.
Description of drawings
Fig. 1 is the amine liquid regeneration technology easy device flow chart of the embodiment of the invention of the single resin bed of employing;
The breakthrough curve of Fig. 2 II type styrene resin heat stable salts changes.When flowing through resin bed with amine liquid, the concentration of heat stable salts is represented with respect to amine liquid elution volume.Resin is at the breakthrough curve of 100 circulations and 2300 circulation times.
Fig. 3 II type styrene resin purifies amine liquid, a step method of reproduction experiment cycle-index and heat stable salts content (HSS%) variation relation figure.
Fig. 4 acrylic resin is with one-step method regeneration tests cycle-index and heat stable salts content (HSS%) variation relation figure.
The specific embodiment
Below in conjunction with accompanying drawing and example the present invention is described in further detail.
Example 1~3
In the glass column of three internal diameter 15mm, be respectively charged into the fresh I type of 30ml styrene resin (A), II type styrene resin (B) and acrylic resin (C).With 5~20% NaOH transition, resin is by Cl -Type converts OH to -Type.Each resin sample is carried out titration with standard hydrochloric acid, is the initial exchange capacity of resin.
Then, five regeneration cycle of every kind of resin experience: making the saturated solution of resin adsorption is the 30%MDEA/ aqueous solution, contain 0.5 milliequivalent KSCN in wherein every gram solution, the resin bed 15 minutes of flowing through is with the NaOH flushing resin regeneration in 60 minutes of 10~20wt%.After each regeneration, mixed with resin is even, measure the exchange capacity of various resins with the standard salt acidometric titration.The exchange capacity of each recycled resin is as shown in table 1.
Three kinds of different resins absorption of table 1 SCN -After the regeneration, the exchange capacity change list:
Cycle-index Example 1 Example 2 Example 3
I type styrene resin (A) II type styrene resin (B) Acrylic resin (C)
Exchange capacity eq/L Percentage % with respect to the initial exchange capacity Exchange capacity eq/L Percentage % with respect to the initial exchange capacity Exchange capacity eq/L Percentage % with respect to the initial exchange capacity
0 1.29 100 1.09 100 1.25 100
1 0.27 21 0.57 52 0.90 71
2 0.22 17 0.54 50 0.89 68
3 0.19 15 0.56 51 0.86 65
4 0.17 13 0.53 49 0.85 66
As can be seen from Table 1, to SCN -The desorption ability acrylic resin best, I type styrene resin desorption ability is the poorest.
Example 4
The 200 milliliters of I type styrene resins (A) of packing in the glass column of internal diameter 20mm wash about 120 minutes transition with 500 milliliters of 5~20wt% NaOH, and resin is by Cl -Type converts OH to -Type.Behind deionized water rinsing, dry up standby with nitrogen.
Purify amine liquid with resin, regeneration cycle 100 times, amine liquid uses 30% oil plant desulfurizer amine liquid of heat stable salts content 5%~10%, makes resin adsorption saturated with 300~900 milliliters of amine liquid, washes resin with the NaOH of 200 milliliters of 5~20wt% and regenerates in 60 minutes.Circulate after 100 times, with the sodium chloride solution flushing of 5~20wt%, with the NaOH flushing, the resin volume obviously expands again, purifies the circulation of amine liquid again.The 1st time, the 100th time and sample of the per 50 milliliters of collections of the 101st the circular flow fluid in saline solution flushing back, the heat stable salts content in the analytic sample.Analyze data such as table 2.
Compare with fresh resin after observing resin circulation 100 times, can not recover after obvious contraction and regeneration are arranged, when handling with sodium chloride, flowing out liquid is pale brown look, and the resin volume obviously expands, and the exchange capacity of handling the back resin recovers substantially, and resuscitation effect is more obvious.
Table 2 is with before and after the sodium chloride recovery resin, and resin removes heat stable salts experimental data table:
The 1st time (HSS%) The 100th time (HSS%) The 101st time (HSS%)
????50ml ????0.03 ????0.51 ????0.05
????100ml ????0.17 ????1.67 ????0.21
????150ml ????0.59 ????5.78 ????0.65
????200ml ????1.45 ????6.10 ????1.58
????250ml ????4.93 ????6.54 ????4.87
????300ml ????6.16 ????6.85 ????6.45
Example 5
In amine liquid purifier shown in Figure 1, in the stainless steel bed of the high 60cm of internal diameter 25mm, add II type styrene resin (B) and purify the experiment of amine liquid, the heat stable salts content in the amine liquid is about 2~6%, with the regeneration of NaOH one-step method.When circulation 100 times and 2300 times, flow out sample of the per 50 milliliters of collections of liquid, the heat stable salts content in the analytic sample.Draw the breakthrough curve of resin, as shown in Figure 2.As can be seen from Figure 2 compare circulation for 2300 times 100 times the time, the ability that removes heat stable salts in the amine liquid of resin obviously descends.
Example 6
In amine liquid purifier shown in Figure 1, in the stainless steel bed of the high 60cm of internal diameter 25mm, add II type styrene resin (B) and purify the experiment of amine liquid, heat stable salts content in the amine liquid is about 2~5%, and 300~900 milliliters of amine liquid of each circularly purifying are with one step of NaOH method of reproduction.About 100 times of every circulation, to analyzing through the heat stable salts content in the amine liquid before and after the resin bed, each product amine liquid need mix.
The experiment situation as shown in Figure 3.As can be seen from Figure 3 II type styrene resin (B) obviously descends in the efficient that circulation removes heat stable salts in the amine liquid after 2200 times.
Getting 5 gram resins, to measure exchange capacities be 0.35eq/L, be new resin exchange capacity (1.09eq/L) 32%.
Example 7
In amine liquid purifier shown in Figure 1, in the stainless steel bed of the high 60cm of internal diameter 25mm, add acrylic resin (C) and purify the experiment of amine liquid, heat stable salts content 2~5% in the amine liquid, 300~900 milliliters of amine liquid of each circularly purifying are with the regeneration of NaOH one-step method.About 100 times of each circulation, to analyzing through the heat stable salts content in the amine liquid before and after the resin bed, each product amine liquid need mix post analysis.
The experiment situation as shown in Figure 4.As can be seen from Figure 4 the efficient of acrylic resin (C) still keeps stronger heat stable salts removal efficiency 3500 circulations.
Example 8
In amine liquid purifier shown in Figure 1, in the stainless steel column of the high 60cm of internal diameter 25mm, add acrylic resin (C) and purify the experiment of amine liquid, heat stable salts content in the amine liquid is about 3%, and 300 milliliters of amine liquid of each circularly purifying are with the regeneration of NaOH one-step method.After experiencing 3500 circulations, getting 5 gram resins, to measure exchange capacities be 0.74eq/L, be fresh resin exchange capacity (1.25eq/L) 59%.
Example 9
In amine liquid purifier shown in Figure 1, in the stainless steel column of the high 60cm of internal diameter 25mm, add acrylic acid series (C) and purify the experiment of amine liquid, heat stable salts content about 3% in the amine liquid, 300 milliliters of amine liquid of each circularly purifying, with NaOH one-step method regeneration, 100~200 circulations are with the sodium chloride solution flushing recovery of 1~20wt%, experience circulate for 3500 times after, getting 5 gram resins, to measure the exchange capacities of resins be 0.96eq/L, be new resin exchange capacity (1.25eq/L) 77%.Wash the service life that recovery can prolong resin with example 8 comparative illustration sodium chloride.
Example 10
In amine liquid purifier shown in Figure 1, in the stainless steel column of the high 60cm of internal diameter 25mm, add II type styrene resin (B) and purify the experiment of amine liquid, heat stable salts content about 2~5% in the amine liquid, 300~900 milliliters of amine liquid of each circularly purifying, with NaOH one-step method regeneration, 50~100 circulations are with sodium chloride solution flushing recovery, experience circulate for 2200 times after, getting 5 gram resins, to measure the exchange capacities of resins be 0.70eq/L, be new resin exchange capacity (1.09eq/L) 64%.Wash the service life that recovery can prolong resin with embodiment 6 comparative illustration sodium chloride.

Claims (10)

1, a kind of method with strong-base anion-exchange resin purification deterioration amine liquid is characterized in that may further comprise the steps:
A, absorption: with temperature is that 30~60 ℃ and the deterioration amine liquid handled are after filtration flowed through and are filled with the resin bed of strong-base anion-exchange resin, and the heat stable salts anion in the resin adsorption deterioration amine liquid is purified deterioration amine liquid;
B, regeneration: after treating that resin adsorption in the described resin bed is saturated, wash described resin bed, make the resin in the described resin bed obtain regeneration and recover adsorption capacity substantially with alkali metal hydroxide aqueous solution;
C, repetition above-mentioned steps a and step b;
D, recovery: whenever carry out above-mentioned steps a and step b the circulation 50~200 times after, wash described resin bed with sodium-chloride water solution, remove the organic matter and the stronger SCN of affinity that are adsorbed on the resin -, to keep the ion exchange capacity of resin.
2, the method for purification deterioration amine liquid according to claim 1 is characterized in that described strong-base anion-exchange resin is I type styrene-divinylbenzene skeleton strong-base anion-exchange resin, II type styrene-divinylbenzene skeleton strong-base anion-exchange resin or acrylic backbone strong-base anion-exchange resin.
3, the method for purification deterioration amine liquid according to claim 1 is characterized in that described filtration treatment comprises at least with active carbon filter to filter.
4, the method for purification deterioration amine liquid according to claim 1 is characterized in that also comprising the heat stable salts analysis on Content in the gained amine liquid after described adsorption treatment, with the time of determining that the ion exchange resin adion reaches capacity.
5,, it is characterized in that described alkali metal hydroxide aqueous solution is that concentration is the sodium hydrate aqueous solution of 10~20wt% according to the method for the described purification deterioration of arbitrary claim amine liquid in the claim 1 to 4.
6, according to the method for the described purification deterioration of arbitrary claim amine liquid in the claim 1 to 4, the concentration that it is characterized in that described sodium-chloride water solution is 1~20wt%.
7, according to the method for the described purification deterioration of arbitrary claim amine liquid in the claim 1 to 4, it is characterized in that the number of described resin bed is at least two, and be arranged in parallel, with carrying out continuously of the purification that realizes deterioration amine liquid; Perhaps, the number of described resin bed is one, and intermittent operation is adopted in the purification of deterioration amine liquid.
8, according to the method for the described purification deterioration of arbitrary claim amine liquid in the claim 1 to 4, it is characterized in that described deterioration amine liquid refers to that the content of heat stable salts wherein is the aqueous solution of one or more hydramine of 1~15%, hydramine comprises MEA, diethanol amine, triethanolamine, diglycolamine, diisopropanolamine (DIPA) and methyl diethanolamine.
9, according to the method for the described purification deterioration of arbitrary claim amine liquid in the claim 1 to 4, it is characterized in that described heat stable salts anion comprises organic acid, sour gas and inorganic acid radical.
10, the method for purification deterioration amine liquid according to claim 9 is characterized in that described organic acid comprises HCOO -, CH 3COO -And oxalate; Described inorganic acid radical comprises SCN -, Cl -, S 2O 3 2-, SO 4 2-And NO 3 -Described sour gas comprises SO 2, CS 2, HCN, COS and polythionic acid.
CNB2004100534700A 2004-08-03 2004-08-03 Method for purifying deterioration amine liquid using highly basic anion exchange resin CN100333823C (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CNB2004100534700A CN100333823C (en) 2004-08-03 2004-08-03 Method for purifying deterioration amine liquid using highly basic anion exchange resin

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CNB2004100534700A CN100333823C (en) 2004-08-03 2004-08-03 Method for purifying deterioration amine liquid using highly basic anion exchange resin

Publications (2)

Publication Number Publication Date
CN1733355A CN1733355A (en) 2006-02-15
CN100333823C true CN100333823C (en) 2007-08-29

Family

ID=36076100

Family Applications (1)

Application Number Title Priority Date Filing Date
CNB2004100534700A CN100333823C (en) 2004-08-03 2004-08-03 Method for purifying deterioration amine liquid using highly basic anion exchange resin

Country Status (1)

Country Link
CN (1) CN100333823C (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101502742B (en) * 2009-02-20 2011-09-07 中国石油化工集团公司 Method for removing thermostable salt in amine liquid for desulphurization

Families Citing this family (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1844460B (en) * 2006-03-02 2010-08-11 厦门大学 Device for electrochemical removal of heat stable salts in desulfurated amine liquid
US7776296B2 (en) * 2006-03-10 2010-08-17 Cansolv Technologies Inc. Regeneration of ion exchangers that are used for salt removal from acid gas capture plants
CN101966424B (en) * 2010-09-09 2013-08-14 攀钢集团钢铁钒钛股份有限公司 Method for removing sulfate ions and chloride ions in organic amine absorbent
CN102125803B (en) * 2010-12-10 2013-05-01 北京科技大学 Method for purifying degraded amine solution
CN102100978B (en) * 2010-12-14 2013-03-13 南京化学试剂有限公司 Method for removing trace anions from alcohol organic solvent by resin method
CN103127745A (en) * 2011-11-23 2013-06-05 北京世博恒业科技有限公司 Purification method for decarburization alcohol amine in CO2 recovery apparatus
CN102489153A (en) * 2011-11-24 2012-06-13 王传良 Method for regenerating tetramethylguanidine hydroxyl acid salt composite desulfurizer in smoke desulfurization
CN103961901B (en) * 2013-01-30 2016-04-06 中国石油天然气股份有限公司 A kind of method removing long-chain carboxylic acid's salt and hydrocarbon in alkanolamine solution
CN103223266A (en) * 2013-04-26 2013-07-31 江苏天宇石化冶金设备有限公司 Resin-exchange amine liquid purifying system
CN103585818A (en) * 2013-11-26 2014-02-19 博恩(南通)石化设备有限公司 Three-stage amine liquid recovery device
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
CN104192946B (en) * 2014-08-12 2017-01-25 江西瑞林电气自动化有限公司 Amine liquid purification control method and device
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
CN105618164A (en) * 2016-03-30 2016-06-01 伊犁川宁生物技术有限公司 Regeneration method of decolorizing resin
CN109200627B (en) * 2017-06-29 2020-12-01 中国石油天然气股份有限公司 Purification method of alcohol amine solution

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5162084A (en) * 1991-10-08 1992-11-10 Conoco Inc. Process for monitoring and controlling an alkanolamine reaction process
CN1096008A (en) * 1994-04-19 1994-12-07 中国石化大庆石油化工总厂研究院 A kind of preparation of ion retardation resin that is used for purifying waste water containing sodium thiocyanate
US5788864A (en) * 1995-02-24 1998-08-04 Mpr Services Amine heat stable salt removal from type II anion exchange resin

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5162084A (en) * 1991-10-08 1992-11-10 Conoco Inc. Process for monitoring and controlling an alkanolamine reaction process
CN1096008A (en) * 1994-04-19 1994-12-07 中国石化大庆石油化工总厂研究院 A kind of preparation of ion retardation resin that is used for purifying waste water containing sodium thiocyanate
US5788864A (en) * 1995-02-24 1998-08-04 Mpr Services Amine heat stable salt removal from type II anion exchange resin

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
201×7强碱性阴离子交换树脂的污染和复苏 殷志宏,杨辉荣,徐和德,华南师院学报自然科学版,第1980年卷第1期 1980 *
201×7强碱性阴离子交换树脂的污染和复苏 殷志宏,杨辉荣,徐和德,华南师院学报自然科学版,第1980年卷第1期 1980;碱性氯化钠复苏阴离子树脂的应用技术 诸慧芬,中国氯碱,第1996年卷第2期 1996 *
碱性氯化钠复苏阴离子树脂的应用技术 诸慧芬,中国氯碱,第1996年卷第2期 1996 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101502742B (en) * 2009-02-20 2011-09-07 中国石油化工集团公司 Method for removing thermostable salt in amine liquid for desulphurization

Also Published As

Publication number Publication date
CN1733355A (en) 2006-02-15

Similar Documents

Publication Publication Date Title
KR101929100B1 (en) METHOD FOR REMOVING SOx FROM GAS WITH COMPOUND ALCOHOL-AMINE SOLUTION
JP5344934B2 (en) Regeneration of ion exchangers used for removal of salts from acid gas capture plants.
Wang et al. Amine reclaiming technologies in post-combustion carbon dioxide capture
JP4881412B2 (en) Carbon dioxide recovery device
Yang et al. Effects of SO2 on CO2 capture using a hollow fiber membrane contactor
AU2009303874B2 (en) Methods and systems for deacidizing gaseous mixtures
US6852144B1 (en) Method for removing COS from a stream of hydrocarbon fluid and wash liquid for use in a method of this type
CN101092576B (en) Method for removing acid gases in cracked gas
CN102266723B (en) Regenerating method and regenerating device for selective catalytic reduction de-nitration catalyst
KR101441512B1 (en) Water wash method and system for a carbon dioxide capture process
BRPI1012594B1 (en) method to eliminate or substantially reduce the emission of amines and alkaline decomposition products from them to the atmosphere
AU762497B2 (en) Process for the reclamation of spent alkanolamine solution
CN101721833B (en) Method for recovering and purifying hydrocarbon wastegas by condensation and adsorption
CN103611419B (en) Corona discharge and liquid phase oxidation remove SO in coal-fired flue-gas 2and NO xmethod
CN106430244B (en) A method of it is recycled from ammonia nitrogen waste water and purifies ammonia
CN101993750B (en) Method for refining liquefied petroleum gas
US6334886B1 (en) Removal of corrosive contaminants from alkanolamine absorbent process
KR100993689B1 (en) Method for separating and recovering carbon dioxide
CN105536486B (en) Ship tail gas denitrating technique and system, desulfurization and denitrification integral process and system
CN102309913B (en) Treatment method for stinky waste gas containing sulfides and hydrocarbons
CN105214625B (en) A kind for the treatment of process of activation lignite and the coking wastewater using the activation lignite
CN102847431B (en) Method for treating claus technical tail gas
US20110243196A1 (en) Multiple redundant gnss synchronization system
CN101450275A (en) Treatment method of odor gas containing sulfur and dust
CN101347708B (en) Method for processing sulphur-containing exhaust air with fetor escaped from storage tank

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
GR01 Patent grant
C14 Grant of patent or utility model
CP01 Change in the name or title of a patent holder

Address after: Zhenhai District, Zhejiang, Ningbo

Patentee after: China Petroleum Chemical Co Zhenhai Refining & Chemical Branch Company

Address before: Zhenhai District, Zhejiang, Ningbo

Patentee before: Zhenhai Refining Chemical Co., Ltd., SINOPEC

C56 Change in the name or address of the patentee

Owner name: CHINA PETROLEUM CHEMICALS CO., LTD. TOWN HAI LIAN

Free format text: FORMER NAME OR ADDRESS: ZHENHAI OIL-REFINING CHEMICALCO., LTD., CHINA PETRO-CHEMICAL CORP.