CN1978345A - Method and apparatus for separating cyclo-hexane oxidation waste alkali - Google Patents
Method and apparatus for separating cyclo-hexane oxidation waste alkali Download PDFInfo
- Publication number
- CN1978345A CN1978345A CN 200510111321 CN200510111321A CN1978345A CN 1978345 A CN1978345 A CN 1978345A CN 200510111321 CN200510111321 CN 200510111321 CN 200510111321 A CN200510111321 A CN 200510111321A CN 1978345 A CN1978345 A CN 1978345A
- Authority
- CN
- China
- Prior art keywords
- buck
- raw material
- water
- cyclohexane
- cyclo
- Prior art date
- Legal status (The legal status 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 status listed.)
- Granted
Links
Images
Landscapes
- Cyclones (AREA)
Abstract
This invention provides a method and a device for separating waste alkali of cyclohexane oxidation liquid by a spiral-flow coalescence serial combination technology, which separates it in three steps in gravity sedimentation tank, a cyclone separator and a coalescence separator to separate it completely, which overcomes the shortcomings of gravity deposition method and the coalescence separation method and prolongs the effective production time of alkyl distillation tower greatly.
Description
Technical field
The present invention relates to cyclo-hexane oxidation waste alkali is carried out isolating method and device, more particularly, the present invention relates to utilize the coalescent series combination technology of eddy flow that cyclo-hexane oxidation waste alkali is carried out isolating method and device.
Background technology
The production process that cyclohexane oxidation is produced pimelinketone comprises: oxidation, decomposition, salkali waste separation, alkane distillation, saponification, refining, dehydrogenation and operations such as recovery of heat and tail gas recycle.In the decomposition course of cyclohexane oxidation technology, because the adding of aqueous sodium hydroxide solution can produce a large amount of waste lye (mainly being yellow soda ash, organic sodium salt and a spot of free sodium hydroxide).If these waste lyes are brought in the follow-up alkane distillation tower with logistics, can cause the reboiler fouling of alkane distillation tower, thereby cause supplies consumption to increase, and the driving cycle of alkane distillation tower can shorten significantly.
At present, extensively adopt gravity settler and coalescer to remove waste lye in the prior art, cyclo-hexane oxidation waste alkali is separated.
Yet use gravity settler realization cyclohexane oxidation solution separates with waste lye, and separation efficiency is low, required time is long and facility investment is big.And, having only macrobead sedimentation effectively, fine particle can't sedimentation.Gravity settling is only effective greater than the water droplet of 50 μ m to particle diameter.Solution after the separating treatment is tangible oyster white by this method.These fine particles only can not reach the purpose of further thoroughly separating waste lye by gravity settling fully by prolonging residence time sedimentation.And with regard to coalescer, though its separation accuracy height, cut diameter can reach 0.1 μ m, easily causes the blocked shortcoming of element when it exists liquid unholiness.Some strainer puts into operation, do not cross several hrs and the high pressure drop that is difficult to accept will occur, and impact resistance is little, can lose separating power when alkali waste water content is big.
For example, for solving the separation problem of cyclo-hexane oxidation waste alkali, adopted the series combination of gravity settling and one-level coarse separation in the prior art.Fig. 1 is the cyclo-hexane oxidation waste alkali separation system figure of available technology adopting.Na in the solution after the separation
+Content can be reduced to 10-20mg/L, effect is apparent in view, thereby has prolonged the continuous operation time of alkane distillation tower greatly, has improved the output of pimelinketone.But, because effective separated space of gravity settling is little, separation accuracy is poor, cause in the material that enters coalescing separator buck content bigger, increased the coalescing separator working load, cause the replacing of flushing and internals very frequent.
Up to now, the method that does not also have proposition to solve the problems of the technologies described above in the prior art.
Therefore, press for develop can be up hill and dale, effectively cyclo-hexane oxidation waste alkali is separated, be fit to the isolation technique of long-term operation.
Summary of the invention
The present invention adopts the coalescent series combination technology of eddy flow that cyclo-hexane oxidation waste alkali is separated, solve the Cyclohexane Oxidation Unit waste lye effectively and separated halfway problem, prolong the effective production time of alkane distillation tower significantly, thereby solved problems of the prior art.
On the one hand, the invention provides and a kind of cyclo-hexane oxidation waste alkali is carried out isolating method, it may further comprise the steps:
(a) water is injected the cyclo-hexane oxidation waste alkali raw material, making the water-content of the cyclohexane oxide solution after the water filling is 0.5-3.0 volume %, and described raw material is carried out the saponification separation separate with washing, make that water mixes with raw material, raw material neutral and alkali material is to water migration and the enrichment of water neutral and alkali material, obtains the mixture of water and raw material;
(b) by gravity settling the water in the step (a) is carried out the first step with the mixture of raw material and separate, separate and remove the buck that contains alkaline matter, obtain to have removed the cyclohexane oxidation solution of 80-90% buck, i.e. the isolating mixture of the first step;
(c) under the pressure drop of 50-200 ℃ temperature, 0.1-0.25MPa, the isolating mixture of the described the first step is carried out the cyclonic separation in second step, further separate and remove the buck that contains alkaline matter, obtain further to have removed the cyclohexane oxidation solution of 50% buck, i.e. isolating mixture of second step;
(d) under the pressure drop of 50-200 ℃ temperature, 0.05-0.15MPa, described isolating mixture of second step is carried out the coarse separation in the 3rd step, separate again and remove the buck that contains alkaline matter, obtain Na
+Residual quantity be lower than the cyclohexane oxidation solution of 5mg/L.
One preferred embodiment in, in step (a), the water-content of cyclohexane oxide solution is 1.0-2.0 volume % after the water filling.
Another preferred embodiment in, in step (c), it is to carry out under the pressure drop of temperature, 0.15MPa at 60-130 ℃ that described second step separates.
Another preferred embodiment in, in step (d), it is to carry out under the pressure drop of temperature, 0.08MPa at 60-130 ℃ that described the 3rd step separates.
On the other hand, the invention provides and a kind of cyclo-hexane oxidation waste alkali is carried out isolating device, this device comprises
(a) gravity settler, it is used for separating removes buck that the cyclo-hexane oxidation waste alkali raw material contains alkaline matter obtaining to have removed the cyclohexane oxidation solution of 80-90% buck, and described gravity settler comprises that a tank body, is used to infeed the outlet that outlet and that the inlet of cyclo-hexane oxidation waste alkali raw material, is used to discharge the buck that contains alkaline matter is used to discharge the cyclohexane oxidation solution that has removed the 80-90% buck;
(b) cyclone separator, it is used for further separating removal cyclo-hexane oxidation waste alkali raw material and contains the buck of alkaline matter to obtain further to have removed the cyclohexane oxidation solution of 50% buck, described cyclone separator comprises a tank body, one is used to have infeeded from removing of gravity settler the inlet of the cyclohexane oxidation solution of 80-90% buck, one is used to discharge the outlet of the buck that contains alkaline matter, an and outlet that is used to discharge the cyclohexane oxidation solution that has further removed 50% buck, wherein, pipe connection is passed through in the inlet of the described cyclohexane oxidation solution that is used to have infeeded from removing of gravity settler the 80-90% buck and the outlet that is used to discharge the cyclohexane oxidation solution that has removed the 80-90% buck of gravity settler;
(c) coalescing separator, it is used for separating removal cyclo-hexane oxidation waste alkali raw material again and contains the buck of alkaline matter to obtain Na
+Residual quantity be lower than the cyclohexane oxidation solution of 5mg/L, described coalescing separator comprises that the outlet and that inlet, that a tank body, is used to have infeeded from further removing of cyclone separator the cyclohexane oxidation solution of 50% buck is used to discharge the buck that contains alkaline matter is used to discharge Na
+Residual quantity be lower than the outlet of the cyclohexane oxidation solution of 5mg/L, wherein, pipe connection is passed through in the inlet of the described cyclohexane oxidation solution that is used to have infeeded from further removing of cyclone separator 50% buck and the outlet that is used to discharge the cyclohexane oxidation solution that has further removed 50% buck of cyclone separator.
One preferred embodiment in, described device also comprise by pipeline and gravity settler be used to infeed the washing separating tank that the inlet of cyclo-hexane oxidation waste alkali raw material is connected, and separate tank connected saponification separating tank with described washing by pipeline.
Another preferred embodiment in, the water flow of described cyclone separator is the 1-5% of its inlet flow rate.
Another preferred embodiment in, described gravity settler adopts single-stage or plural serial stage.
Another preferred embodiment in, described cyclone separator adopts single-stage or plural serial stage.
Another preferred embodiment in, described coalescing separator adopts single-stage or plural serial stage.
Description of drawings
Fig. 1 is the synoptic diagram of the cyclo-hexane oxidation waste alkali separation system of available technology adopting.
Fig. 2 is the synoptic diagram of gravity settler, cyclone separator and coalescing separator combination separation process according to one embodiment of the present invention.
Fig. 3 is the synoptic diagram of gravity settler, two-stage cyclone separator and the coalescing separator combination separation process of another embodiment according to the present invention.
Wherein, Reference numeral 10,20,30,40 and 50 is represented following equipment respectively:
10: the saponification separating tank
20: the washing separating tank
30: gravity settler
40: coalescing separator
50: cyclone separator.
Embodiment
The present inventor finds after having passed through extensive and deep research, by be used in combination gravity settler, cyclone separator and coalescing separator to cyclo-hexane oxidation waste alkali carry out three the step separate, can solve effectively that the Cyclohexane Oxidation Unit waste lye separates halfway problem in the prior art, overcome shortcomings such as the flushing of the undesirable and coarse separation method of existing settling methods effect is frequent, prolong the effective production time of alkane distillation tower significantly, thereby significantly reduced production cost.Based on above-mentioned discovery, the present invention is accomplished.
Technical conceive of the present invention is as follows: since the height of the separation accuracy force of gravity slurry tank of cyclone separator (its cut diameter is 10 μ m, the buck content of the cyclohexane oxide solution of handling can be 0.1-30%, turndown ratio is bigger), (its cut diameter is 0.1 μ m and the separation accuracy of coalescing separator is than the height of cyclone separator, but the buck content of the cyclohexane oxide solution of handling can not be too high, it is coalescent that the too high meeting of buck content has little time the buck particle, causes separation efficiency to descend.Industrial practice proves, gravity settler and coalescing separator series connection use are removed the buck in the cyclohexane oxide solution, gravity settler outlet is that the buck content of cyclohexane oxide solution of coalescing separator import is still than higher, separation to coalescing separator is unfavorable), therefore, if single-stage or multistage cyclone separator are set between gravity settler and coalescing separator, can reduce the buck content of the cyclohexane oxide solution of coalescing separator import, improve the treatment effect of coalescing separator greatly, thereby reduce the buck content of the cyclohexane oxide solution of coalescing separator outlet.The present invention fully takes into account the characteristics of gravity settler, cyclone separator and coalescing separator, at first with gravity settler the buck in the cyclohexane oxide solution being carried out the first step separates, then separate to carry out for second step with the buck particle of cyclone separator processing particle diameter greater than 10 μ m, handling the fewer particle diameter of content with coalescing separator at last separates to carry out for the 3rd step less than the buck particle of 10 μ m, the effective combination of three is handled the buck of cyclohexane oxide solution, improved separating effect.
Below, further set forth the present invention in conjunction with the accompanying drawings.
Fig. 2 shows gravity settler, cyclone separator and the coalescing separator combination separation process according to one embodiment of the present invention.At first, water is injected the cyclohexane oxide solution raw material so that the water-content of the cyclohexane oxide solution after the water filling reaches about 0.5-3.0 volume %, preferably about 1.0-2.0 volume %, then it is sent into and carry out saponification in saponification separating tank 10 and the washing separating tank 20 and separate with washing and separate, water mixes with the raw material disperse to finish, raw material neutral and alkali material moves and the enrichment of water neutral and alkali material to water, obtains the mixture of cyclohexane oxide solution raw material and water.Secondly, after treating that cyclohexane oxide solution raw material and water thorough mixing, alkaline matter and water fully transmit, the mixture of cyclohexane oxide solution raw material and water is sent in the gravity settler 30 (optionally, can mend into a certain amount of water) separate to carry out the first step, separate and remove the buck that contains alkaline matter, acquisition has removed the cyclohexane oxidation solution of about 80-90% buck, i.e. the isolating mixture of the first step.Once more, to send in the cyclone separator 50 through the isolating mixture of the first step, under the pressure drop of about 50-200 ℃ temperature, about 0.1-0.25MPa, carry out the cyclonic separation in second step, further separate and remove the buck that contains alkaline matter, obtain further to have removed the cyclohexane oxidation solution of about 50% buck, i.e. isolating mixture of second step.Then, will send in the coalescing separator 40, under the pressure drop of about 50-200 ℃ temperature, about 0.05-0.15MPa, carry out the coarse separation in the 3rd step, and separate again and remove the buck that contains alkaline matter, obtain Na through isolating mixture of second step
+Residual quantity be lower than the cyclohexane oxidation solution of about 5mg/L, i.e. cyclohexane oxidation solution of Jing Huaing.The cyclohexane oxidation solution of described purification can be sent in downstream unit such as the alkane distillation tower and be used for further processing.
The cyclone pipe that described cyclone separator adopts can a shared feed cavity, an oil phase outlet plenum, an oily(waste)water outlet plenum, described feed cavity and outlet plenum can be three independent containers, also can be three parts in the container, to simplify the structure of production equipment.
Can be used for cyclone separator of the present invention can be the various cyclone separators of this area routine.Cyclone separator can be a single-stage or multistage.A kind of constructional feature of preferred cyclone separator and principle can referring to, for example Chinese patent ZL 00217613.0.
The gravity settler that uses among the present invention is had no particular limits, and can be the conventional various gravity settlers that use in the cyclo-hexane oxidation waste alkali separation field.Gravity settler can be a single-stage or multistage, uses three grades of placed in-line gravity settlers usually.
The coalescing separator that uses among the present invention is also had no particular limits, and can be the conventional various coalescing separators that use in the cyclo-hexane oxidation waste alkali separation field.Coalescing separator can be a single-stage or multistage.
Above-mentioned separation has adopted gravity settling, cyclonic separation and coarse separation bonded technology to the dealkalize of cyclohexane oxidation solution, this technology fully take into account the cyclone separator turndown ratio big, be difficult for blocking, to the macrobead good separating effect, and the coalescing separator internals are not suitable for long-term operation, to the characteristics of fine particle good separating effect.Carrying out the first step by gravity settler earlier separates; Then adopting cyclone separator to carry out for second step separates to remove macrobead; Behind working load that greatly reduces coalescing separator and running cost, utilize coalescing separator to carry out for the 3rd step again and separate (segmentation from), thereby improved separating effect.Those skilled in the art can determine that cyclone separator and/or coalescing separator adopt single-stage or plural serial stage according to the separating effect of reality, in the hope of reaching optimal effect.
Service temperature to cyclone separator and coalescing separator has no particular limits, and those skilled in the art can make the selection that corresponds to actual needs flexibly according to the production needs of reality.Described temperature is about 50-200 ℃ usually, preferably about 60-130 ℃.The operation pressure drop of cyclone separator is about 0.1-0.25MPa usually, preferably about 0.15MPa; The operation pressure drop of coalescing separator is about 0.05-0.15MPa usually, preferably about 0.08MPa.
Fig. 3 shows gravity settler, two-stage cyclone separator and the coalescing separator combination separation process of another embodiment according to the present invention.Its operating process is same as shown in Figure 2, and just cyclone separator has adopted two-stage series connection.At first, water is injected the cyclohexane oxide solution raw material so that the water-content of the cyclohexane oxide solution after the water filling reaches about 0.5-3.0 volume %, preferably about 1.0-2.0 volume %, then it is sent into and carry out saponification in saponification separating tank 10 and the washing separating tank 20 and separate with washing and separate, water mixes with the raw material disperse to finish, raw material neutral and alkali material moves and the enrichment of water neutral and alkali material to water, obtains the mixture of cyclohexane oxide solution raw material and water.Secondly, after treating that cyclohexane oxide solution raw material and water thorough mixing, alkaline matter and water fully transmit, the mixture of cyclohexane oxide solution raw material and water is sent in the gravity settler 30 (optionally, can mend into a certain amount of water) separate to carry out the first step, separate and remove the buck that contains alkaline matter, acquisition has removed the cyclohexane oxidation solution of about 80-90% buck, i.e. the isolating mixture of the first step.Once more, to send into successively in first step cyclone separator 50 and the second stage cyclone separator 50 through the isolating mixture of the first step, under the pressure drop of about 50-200 ℃ temperature, about 0.1-0.25MPa, carry out the cyclonic separation in second step, further separate and remove the buck that contains alkaline matter, obtain further to have removed the cyclohexane oxidation solution of about 50% buck, i.e. isolating mixture of second step.Then, will send in the coalescing separator 40, under the pressure drop of about 50-200 ℃ temperature, about 0.05-0.15MPa, carry out the coarse separation in the 3rd step, and separate again and remove the buck that contains alkaline matter, obtain Na through isolating mixture of second step
+Residual quantity be lower than the cyclohexane oxidation solution of about 5mg/L, i.e. cyclohexane oxidation solution of Jing Huaing.The cyclohexane oxidation solution of described purification can be sent in downstream unit such as the alkane distillation tower and be used for further processing.
Major advantage of the present invention is:
(a) with cyclone separation process and Coalescence-separation Technology series combination, given full play to that cyclonic separation is good at roughing out, coarse separation is good at thin isolating characteristics, thereby, existing cyclohexane oxidation solution dealkalize operation of equipment cost height, the unfavorable shortcoming of separating effect have been overcome by more rational gradient distribution separation method.
(b) though because of having increased the increase that cyclone separator causes facility investment, the effective production time by prolonging the alkane distillation tower has significantly also reduced maintenance cost, thereby has reduced production cost significantly, has increased output.Calculate with 400 tons of/hour tripping devices, only 10% cyclone separator equipment drops into, and can produce 2,000 ten thousand yuan economic benefit in 1 year.
(c) production equipment of the present invention is simple in structure, implement easily, easy to operate, and suitable long-term operation, be applicable to cyclo-hexane oxidation waste alkali is separated, also be applicable to the liquid-liquid separation that device is immiscible or solubleness is very low such as oil-refining chemical, be adapted at promoting the use of on the petroleum chemical industry.
(d) application of the present invention can make the gravity settler volume reduce about 50-60%, has saved great deal of steel, has reduced the purging number of times, has saved energy consumption.
Below in conjunction with specific embodiment, further set forth the present invention.Should be understood that these embodiment only to be used to the present invention is described and be not used in and limit the scope of the invention.The experimental technique of unreceipted actual conditions in the following example, usually according to normal condition, or the condition of advising according to manufacturer.Unless indicate, otherwise all umbers are parts by weight that all per-cents are weight percentage.
Embodiment 1
By gravity settler shown in Figure 2, cyclone separator and coalescing separator combination separation process, cyclo-hexane oxidation waste alkali is separated, wherein
(1) material properties
The material that adopts is organic phase and inorganic mixture mutually.Rated flow is about 275 tons/hour, and temperature is about 95-115 ℃, and medial temperature is about 105 ℃.
Density: organic phase on average is about 856.4kg/m
3, the inorganic density of water in the time of 105 ℃ of pressing mutually is about 954.7kg/m
3
Viscosity: organic phase on average is about 0.665 * 10
-3Pas.
(2) assay
Na
+Content adopt atomic absorption spectroscopy determination.The content of water adopts chromatography determination.
(3) effect
(a) after the system applies, avoided effectively being forced to the parking of alkane distillation tower is cleaned because of the fouling of band alkali, alkane distillation tower wash number is reduced to 2 times/year by 5 times/year of independent use coalescing separator, has improved pimelinketone output, has reduced pimelinketone consumption, and remarkable economic efficiency is arranged.
(b) equipment volume has reduced about 50-60%.
(c) when import buck content is not more than about 1600mg/L, adopt that buck content on average reaches below about 150mg/L Na in the organic phase after the flow processing shown in Figure 2
+Content be reduced to below about 5mg/L.
By the placed in-line flow process of employing two-stage cyclone separator shown in Figure 3 cyclo-hexane oxidation waste alkali is separated, wherein
(1) material properties
Material is organic phase and inorganic mixture mutually.Rated flow is about 180 tons/hour, and temperature is about 95-115 ℃, on average is about 105 ℃.
Density: organic phase on average is about 856.4kg/m
3, the inorganic density of water in the time of 105 ℃ of pressing mutually is about 954.7kg/m
3
Viscosity: organic phase on average is about 0.665 * 10
-3Pas.
(2) assay
Na
+Content adopt atomic absorption spectroscopy determination.The content of water adopts chromatography determination.
(3) effect
(a) after the system applies, avoided effectively being forced to the parking of alkane distillation tower is cleaned because of the fouling of band alkali, alkane distillation tower wash number is reduced to 2 times/year by 5 times/year of independent use coalescing separator, has improved pimelinketone output, has reduced pimelinketone consumption, and remarkable economic efficiency is arranged.
(b) equipment volume reduces about 50-60%.
(c) when import buck content is not more than about 50000mg/L, adopt that buck content on average reaches below about 150mg/L Na in the organic phase after the flow processing shown in Figure 3
+Content be reduced to below about 5mg/L.
As can be seen, the inventive method can be with the Na in the cyclohexane oxide solution from the foregoing description
+Content is reduced to below about 5mg/L by about 50-100mg/L, and buck content can be reduced to below about 150mg/L.Therefore, the present invention has solved the Cyclohexane Oxidation Unit waste lye effectively and has separated halfway problem, has prolonged the continuous operation time of alkane distillation tower significantly.
Though for the purpose that is aware and understand, the present invention is described in detail, but after having read present specification, those skilled in the art will be appreciated that, under the prerequisite that does not depart from spirit of the present invention and essence, can carry out various modifications and change to the present invention, these modifications and change all fall within the included scope of appended claims and content of equal value thereof.
Claims (10)
1. one kind is carried out isolating method to cyclo-hexane oxidation waste alkali, and it may further comprise the steps:
(a) water is injected the cyclo-hexane oxidation waste alkali raw material, making the water-content of the cyclohexane oxide solution after the water filling is 0.5-3.0 volume %, and described raw material is carried out the saponification separation separate with washing, make that water mixes with raw material, raw material neutral and alkali material is to water migration and the enrichment of water neutral and alkali material, obtains the mixture of water and raw material;
(b) by gravity settling the water in the step (a) is carried out the first step with the mixture of raw material and separate, separate and remove the buck that contains alkaline matter, obtain to have removed the cyclohexane oxidation solution of 80-90% buck, i.e. the isolating mixture of the first step;
(c) under the pressure drop of 50-200 ℃ temperature, 0.1-0.25MPa, the isolating mixture of the described the first step is carried out the cyclonic separation in second step, further separate and remove the buck that contains alkaline matter, obtain further to have removed the cyclohexane oxidation solution of 50% buck, i.e. isolating mixture of second step;
(d) under the pressure drop of 50-200 ℃ temperature, 0.05-0.15MPa, described isolating mixture of second step is carried out the coarse separation in the 3rd step, separate again and remove the buck that contains alkaline matter, obtain Na
+Residual quantity be lower than the cyclohexane oxidation solution of 5mg/L.
2. the method for claim 1 is characterized in that, in step (a), the water-content of cyclohexane oxide solution is 1.0-2.0 volume % after the water filling.
3. the method for claim 1 is characterized in that, in step (c), it is to carry out under the pressure drop of temperature, 0.15MPa at 60-130 ℃ that described second step separates.
4. the method for claim 1 is characterized in that, in step (d), it is to carry out under the pressure drop of temperature, 0.08MPa at 60-130 ℃ that described the 3rd step separates.
5. one kind is carried out isolating device to cyclo-hexane oxidation waste alkali, and it comprises
(a) gravity settler (30), it is used for separating removes buck that the cyclo-hexane oxidation waste alkali raw material contains alkaline matter obtaining to have removed the cyclohexane oxidation solution of 80-90% buck, and described gravity settler (30) comprises that a tank body, is used to infeed the outlet that outlet and that the inlet of cyclo-hexane oxidation waste alkali raw material, is used to discharge the buck that contains alkaline matter is used to discharge the cyclohexane oxidation solution that has removed the 80-90% buck;
(b) cyclone separator (50), it is used for further separating removal cyclo-hexane oxidation waste alkali raw material and contains the buck of alkaline matter to obtain further to have removed the cyclohexane oxidation solution of 50% buck, described cyclone separator (50) comprises a tank body, one is used to have infeeded from removing of gravity settler (30) inlet of the cyclohexane oxidation solution of 80-90% buck, one is used to discharge the outlet of the buck that contains alkaline matter, an and outlet that is used to discharge the cyclohexane oxidation solution that has further removed 50% buck, wherein, pipe connection is passed through in the inlet of the described cyclohexane oxidation solution that is used to have infeeded from removing of gravity settler (30) the 80-90% buck and the outlet that is used to discharge the cyclohexane oxidation solution that has removed the 80-90% buck of gravity settler (30);
(c) coalescing separator (40), it is used for separating removal cyclo-hexane oxidation waste alkali raw material again and contains the buck of alkaline matter to obtain Na
+Residual quantity be lower than the cyclohexane oxidation solution of 5mg/L, described coalescing separator (40) comprises that the outlet and that inlet, that a tank body, is used to have infeeded from further removing of cyclone separator (50) the cyclohexane oxidation solution of 50% buck is used to discharge the buck that contains alkaline matter is used to discharge Na
+Residual quantity be lower than the outlet of the cyclohexane oxidation solution of 5mg/L, wherein, pipe connection is passed through in the inlet of the described cyclohexane oxidation solution that is used to have infeeded from further removing of cyclone separator (50) 50% buck and the outlet that is used to discharge the cyclohexane oxidation solution that has further removed 50% buck of cyclone separator (50).
6. device as claimed in claim 5, it is characterized in that, it also comprises and is used to infeed the washing separating tank (20) that the inlet of cyclo-hexane oxidation waste alkali raw material is connected, and the saponification separating tank (10) that is connected with described washing separating tank (20) by pipeline by pipeline and gravity settler (30).
7. device as claimed in claim 5 is characterized in that, the water flow of described cyclone separator (50) is the 1-5% of its inlet flow rate.
8. device as claimed in claim 5 is characterized in that, described gravity settler (30) adopts single-stage or plural serial stage.
9. device as claimed in claim 5 is characterized in that, described cyclone separator (50) adopts single-stage or plural serial stage.
10. device as claimed in claim 5 is characterized in that, described coalescing separator (40) adopts single-stage or plural serial stage.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200510111321XA CN100503477C (en) | 2005-12-09 | 2005-12-09 | Method and apparatus for separating cyclo-hexane oxidation waste alkali |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200510111321XA CN100503477C (en) | 2005-12-09 | 2005-12-09 | Method and apparatus for separating cyclo-hexane oxidation waste alkali |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1978345A true CN1978345A (en) | 2007-06-13 |
| CN100503477C CN100503477C (en) | 2009-06-24 |
Family
ID=38129686
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200510111321XA Active CN100503477C (en) | 2005-12-09 | 2005-12-09 | Method and apparatus for separating cyclo-hexane oxidation waste alkali |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100503477C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101108794B (en) * | 2007-08-16 | 2010-05-19 | 华东理工大学 | Method for prolonging cycle of oparation of pimelinketone device and equipment thereof |
| CN101734689A (en) * | 2008-11-27 | 2010-06-16 | 华东理工大学 | Method and device for separating and recycling alkali waste in cyclohexane oxide solution |
| CN102302868A (en) * | 2011-07-13 | 2012-01-04 | 化学工业第二设计院宁波工程有限公司 | Alkali waste separating device and method in process of preparing cyclohexanone and cyclohexanol by oxidization of cyclohexane |
-
2005
- 2005-12-09 CN CNB200510111321XA patent/CN100503477C/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101108794B (en) * | 2007-08-16 | 2010-05-19 | 华东理工大学 | Method for prolonging cycle of oparation of pimelinketone device and equipment thereof |
| CN101734689A (en) * | 2008-11-27 | 2010-06-16 | 华东理工大学 | Method and device for separating and recycling alkali waste in cyclohexane oxide solution |
| CN101734689B (en) * | 2008-11-27 | 2013-08-07 | 华东理工大学 | Method and device for separating and recycling alkali waste in cyclohexane oxide solution |
| CN102302868A (en) * | 2011-07-13 | 2012-01-04 | 化学工业第二设计院宁波工程有限公司 | Alkali waste separating device and method in process of preparing cyclohexanone and cyclohexanol by oxidization of cyclohexane |
| CN102302868B (en) * | 2011-07-13 | 2013-07-10 | 重庆华峰化工有限公司 | Alkali waste separating device and method in process of preparing cyclohexanone and cyclohexanol by oxidization of cyclohexane |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100503477C (en) | 2009-06-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101734689B (en) | Method and device for separating and recycling alkali waste in cyclohexane oxide solution | |
| CN101070507B (en) | Regeneration method for waste lubricant and apparatus | |
| CN101962566B (en) | Mercaptan removed alkali liquid oxidation regeneration method and device thereof | |
| CN101108794B (en) | Method for prolonging cycle of oparation of pimelinketone device and equipment thereof | |
| CN1919818A (en) | Method of recovery phenol from waste water and system thereof | |
| CN102302868B (en) | Alkali waste separating device and method in process of preparing cyclohexanone and cyclohexanol by oxidization of cyclohexane | |
| CN100503477C (en) | Method and apparatus for separating cyclo-hexane oxidation waste alkali | |
| CN101792224B (en) | Method and device for processing emptied water of delayed coking | |
| CN109825322B (en) | Method for extracting phenolic substances from coal tar or direct coal liquefaction oil | |
| CN111686950B (en) | Method and device for quickly separating oil from water at high temperature and high pressure | |
| CN101302438B (en) | Method and apparatus for removing alkali in acid soluble oil containing alkaline impurities | |
| CN211226451U (en) | Coal chemical wastewater extraction deoiling equipment | |
| CN102234248A (en) | Impurity extraction method for caprolactam production | |
| Liu et al. | Cooperative physical separation of oil and suspended solids from methanol-to-olefin wastewater: A pilot study | |
| CN104629794A (en) | Oil-gas-washing-coupled oil-water initial separation method and device | |
| CN101795980A (en) | Method for treatment of water comprising non-polar compounds | |
| CN104291273A (en) | Aromatic hydrocarbon extracting device applied behind hydrogen peroxide extraction column and aromatic hydrocarbon extracting technology | |
| CN204745744U (en) | Liquid -liquid separation coalescer | |
| CN101811785A (en) | Method and device for delaying coking unwatering cyclone decoking | |
| CN201071357Y (en) | Primary oil depickling system | |
| CN220223918U (en) | Device for reducing COD (chemical oxygen demand) of acidic water at top of catalytic fractionation tower | |
| CN105460902B (en) | A kind of discharge piece-rate system suitable for Hydrogen Peroxide Production | |
| CN214936479U (en) | Novel atmospheric and vacuum electro-desalting sewage deep oil-water separation equipment | |
| CN219314771U (en) | Oil field dirty oil, oily waste liquid and ageing oil treatment device | |
| CN214087944U (en) | Coal chemical industry wastewater pretreatment device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |