CN115025506B - Dynamic concentration distillation method of distillation recovery system - Google Patents
Dynamic concentration distillation method of distillation recovery system Download PDFInfo
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- CN115025506B CN115025506B CN202210180651.8A CN202210180651A CN115025506B CN 115025506 B CN115025506 B CN 115025506B CN 202210180651 A CN202210180651 A CN 202210180651A CN 115025506 B CN115025506 B CN 115025506B
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- 238000004821 distillation Methods 0.000 title claims abstract description 119
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000011084 recovery Methods 0.000 title description 11
- 239000007788 liquid Substances 0.000 claims abstract description 54
- 239000010865 sewage Substances 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 4
- 239000000295 fuel oil Substances 0.000 claims description 3
- 238000011109 contamination Methods 0.000 claims description 2
- 230000001502 supplementing effect Effects 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 4
- 238000004134 energy conservation Methods 0.000 abstract description 3
- 238000004140 cleaning Methods 0.000 description 23
- 239000002904 solvent Substances 0.000 description 13
- 239000004215 Carbon black (E152) Substances 0.000 description 12
- 229930195733 hydrocarbon Natural products 0.000 description 12
- 150000002430 hydrocarbons Chemical class 0.000 description 12
- 239000003921 oil Substances 0.000 description 5
- 238000001944 continuous distillation Methods 0.000 description 4
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- 230000003749 cleanliness Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000013020 steam cleaning Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/02—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in boilers or stills
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The application discloses a dynamic concentration distillation method, wherein at least one concentration tank is communicated with a distillation tank through a pipeline with a valve; after the distillation tank continuously distills for a period of time, part of the dirty liquid in the distillation tank is led into the concentration tank for concentration, so that the distillation tank is not stopped for concentrating and distilling, the concentrated liquid is distilled and boiled in the concentration tank more thoroughly, and meanwhile, the total discharge amount of the waste liquid can be reduced, and the aim of reducing emission is achieved; in addition, through an electric control means, an optimal balance point Z can be found through the change rate of the volume and time, so that 2 key values of an optimal liquid discharge time point delta tx and the concentration times n are found, different distillation combination schemes are selected by setting conditions, and the purposes of energy conservation are achieved while the optimal distillation combination is intelligently selected.
Description
Technical Field
The application relates to the field of precision part cleaning, in particular to an improvement of a distillation recovery system.
Background
The precision cleaning field has higher requirements on cleanliness, and the cleaning mode can be divided into water aqua cleaning and solvent cleaning. The greasy dirt on the surface of the parts to be cleaned during solvent cleaning is dissolved in the solvent, and in addition, in solvent cleaning equipment, steam cleaning is often performed before drying to perform final cleaning. At present, most solvents for cleaning are environment-friendly solvents, namely hydrocarbon cleaning solvents, and all automatic cleaners using hydrocarbon solvents are generally called hydrocarbon cleaners, and the type of cleaners are basically provided with a negative pressure distillation recovery system for purifying renewable cleaning agents and providing steam required for cleaning.
The source of the distillation recovery liquid is the liquid with the most oil-containing dirt in the cleaning liquid circulation system, and the pure hydrocarbon solvent is evaporated and consumed by steam cleaning in the distillation process and is cooled and recovered into pure hydrocarbon liquid, and the pure hydrocarbon liquid flows back into the hydrocarbon cleaning system. However, after the distillation is continued for a period of time, the enriched greasy dirt in the distillation recovery tank is more and more, the hydrocarbon steam quantity and the quality are poorer, the cleaning operation is stopped, the liquid in the distillation tank is completely distilled, the greasy dirt is discharged out of the distillation tank, and the cleaning operation is performed after the complete distillation is finished.
The conventional distillation recovery method cannot meet the cleaning condition with high cleanliness requirement, and the distillation method for suspending the cleaning operation cannot meet the high-efficiency operation occasion of cleaning without stopping.
Disclosure of Invention
The application aims to overcome the defect that the liquid in a distillation tank is completely distilled by stopping at intervals during hydrocarbon cleaning in the prior art, and provides a dynamic concentration distillation method of a distillation recovery system.
In order to solve the technical problems, the application provides the following technical scheme:
the application relates to a dynamic concentration distillation method of a distillation recovery system, which is characterized in that the dynamic concentration distillation system is improved.
After distilling in the distillation tank for a period of time, the precipitated greasy dirt in the distillation tank is more and more, the quantity of hydrocarbon steam is less and less, the quality is also deteriorated, the normal cleaning beat is affected, the cleaning operation in the system is stopped, the liquid in the distillation tank is concentrated and distilled at the moment, the greasy dirt is discharged out of the distillation tank, and the cleaning operation is carried out after the completion of the greasy dirt. The process is to stop the machine and distill and boil.
The application designs a concentrating tank below the distilling tank, when the distilling tank above distills for a period of time, the concentrating tank is pumped with negative pressure to ensure that the distilling tank and the concentrating tank form pressure difference, the liquid in the distilling tank is led into the concentrating tank through a valve V1, the liquid is boiled in the concentrating tank, and meanwhile, the distilling tank is continuously supplemented with the sewage for continuous distillation. Because of the existence of the concentration tank, the dirty liquid led into the distillation tank can be continuously boiled to be dry, and the distillation tank can be continuously distilled to generate steam for normal cleaning operation. Thus realizing the distillation boiling without stopping the machine. And the bottom of the distillation tank is always provided with a place which can not be covered completely by the heater, the boiling is not thorough, the discharge amount of each time is more, after the distillation tank with smaller volume is newly added, the dirty liquid can be fully concentrated and distilled, the recovery amount of hydrocarbon is improved, the discharge of waste liquid is reduced, and the energy is really saved and the environment is protected.
When the sewage is fed into the distillation tank by the negative pressure generated by the vacuum unit, the distillation tank heating system provides heat required by distillation, the distillation process is started, a plurality of concentrating tanks are arranged at the bottom of the distillation tank, and heaters required by concentration distillation are respectively arranged in each concentrating tank.
In addition, the concentration process can select the optimal distillation combination through intelligent control of electric control, and accordingly energy conservation is achieved. The specific control method is exemplified below:
assuming that the liquid amount represented by the liquid level supplied to the concentration tank is V2 and the liquid amount supplied to the stop position is V1, the distillation amount per time is Δv=v1-V2, the distillation time required for distillation from V1 to V2 per time is Δt, and the rate of change of the distillation amount and the distillation time is K,then in the case of a constant artificial control of the distillation quantity DeltaV, the K value is inversely proportional to Deltat, i.e. the smaller the K value the greater Deltat; the corresponding rate of change K of distillation amount and distillation time is determined by the mass of hydrocarbon solvent, msolvent, and the mass of greasy dirt, moil. Can be represented by the following formula: />
When the oil stain in the liquid is more, the smaller the K value is, the larger the distillation time delta t is, and in summary, the relative change curve of K and delta t can be obtained as shown in figure 2;
therefore, an optimal balance point is found according to experiments and detection, and the value of the distillation time Deltatx corresponding to the Z point can be obtained on the assumption that the position of Z in the graph, namely, when the distillation time Deltatx is more than or equal to Deltatx, the time point can be set as a liquid discharge time point, which indicates that the oil content in distilled sewage reaches a certain concentration (such as 75%), the distillation time is longer and longer, and the energy consumption required for continuous distillation is far greater than the solvent amount which can be generated by continuous distillation. At this time, there is no need to re-distill, and the distillation is restarted after the dirty liquid is re-supplemented by completely discharging the liquid in the concentration tank 2 through the bottom valve V2. The above process is a whole concentration cycle.
Assuming that the first distillation amount is denoted by Δv1, and the time taken for the first distillation of Δv1 is Δt1, then the following correspondence equation can be obtained by analogy:
ΔV1…………Δt1＜Δtx
ΔV2…………Δt2＜Δtx
ΔV3…………Δt3＜Δtx
ΔV4…………Δt4＜Δtx
…………
when the liquid is replenished for a certain number of times, the following formula appears when the liquid is replenished for the nth time
ΔVn…………Δtn≥Δtx
The controller will then intelligently control the calculated value of n.
Assuming that when n is less than or equal to 4, deltan is less than Deltx, representing light pollution, the work of only opening the concentration tank A is enough;
when n is more than 4, deltan is more than or equal to Deltan, which represents heavy oil stain, and the concentration tank B can be controlled to be opened in a program to enable the two concentration tanks to work simultaneously, so that the efficiency is improved. (PS: the above-mentioned 4 is only a hypothetical value, and this value is set to a reasonable value, and the degree of contamination of the concentrate can be judged to determine the opening of several concentration tanks.)
In the case of an extreme case, if when n=1, Δtn is greater than or equal to Δtx, that is, the time taken for the distillation of the first fed liquid exceeds the set balance point, it proves that the inside of the distillation tank body is heavy oil, and at this time, the distillation tank and the heaters 1-1,2-1,3-1 in the 2 concentration tanks are all turned on, and the whole distillation concentration is stopped.
It is also possible to infer 2 extremes.
Case one: when msolvent=0, k=0, Δtn→infinity, which means that when the solvent is not contained in the liquid and the oil is all, the distillation time tends to be infinite, and in fact, distillation is not necessary at this time, and all the oil can be directly discharged.
And a second case: when moil=0, k=1; delta tn < delta tx, which indicates that when the oil-free liquid is solvent, the concentration time delta tn is always smaller than the distillation time delta tx corresponding to the balance point Z, and then distillation is continuously performed without liquid discharge. In fact this is not necessary and it may be provided to stop the distillation when n reaches a certain number.
Above, can find the optimal equilibrium point Z through the volume with the rate of change of time so as to find the 2 key values of optimal flowing back time Deltatx and concentrated number of times n, and then set up the condition and select different distillation combination schemes, thereby avoid 2 groups to boil and dry the energy waste that the jar is all kept open from beginning to end and cause. The purpose of saving energy is also realized.
The beneficial effects achieved by the application are as follows: the application provides a dynamic concentration distillation method, which can realize non-stop concentration distillation of a distillation recovery system by arranging a concentration tank, so that concentrated solution is distilled and boiled in the concentration tank more thoroughly, and meanwhile, the total discharge amount of waste liquid can be reduced, thereby achieving the aim of reducing emission; in addition, through an electric control means, an optimal balance point Z can be found through the change rate of the volume and time, so that 2 key values of an optimal liquid discharge time point delta tx and the concentration times n are found, different distillation combination schemes are selected by setting conditions, and the purposes of energy conservation are achieved while the optimal distillation combination is intelligently selected.
Drawings
The accompanying drawings are included to provide a further understanding of the application and are incorporated in and constitute a part of this specification, illustrate the application and together with the embodiments of the application, serve to explain the application. In the drawings:
FIG. 1 is a schematic diagram of the structure of the present application;
fig. 2 is a graph of the relative change of K versus Δt.
Detailed Description
The preferred embodiments of the present application will be described below with reference to the accompanying drawings, it being understood that the preferred embodiments described herein are for illustration and explanation of the present application only, and are not intended to limit the present application.
Examples
A dynamic concentration distillation method is characterized in that a small-volume concentration tank is additionally arranged on a distillation tank.
As shown in fig. 1, the distillation tank 1 is respectively communicated with the concentration tank A2 and the concentration tank B3 through pipelines, and valves are arranged on the pipelines. The distillation tank 1 is connected with a distillation tank vacuum unit 1-2, and a concentration tank A heater 2-1 and a concentration tank B heater 3-1 are arranged in the concentration tank A2 and the concentration tank B3; a distillation tank heating system 1-1 is arranged in the distillation tank 1
After distilling in the distillation tank 1 for a period of time, negative pressure is pumped to the concentration tank A2, so that the distillation tank 1 and the concentration tank 2 form a pressure difference, liquid in the distillation tank 1 is led into the concentration tank A2 through a valve, the liquid is boiled in the concentration tank A2, and the distillation tank 1 continuously supplements the sewage for continuous distillation.
Setting a liquid level detection device on the concentration tank A2, setting the liquid amount when the concentration tank A2 starts to supplement liquid level as V2 and the liquid amount when the concentration tank A2 is supplemented to a supplement stop position as V1, wherein the distillation amount of each time is DeltaV=V1-V2;
the distillation time required for each distillation from the V1 position to the V2 position is Δt, assuming that the rate of change of the distillation amount and the distillation time is K; and setting a threshold value of delta t, and when delta t is more than or equal to the threshold value, discharging all the liquid in the concentration tank A2 to complete one concentration period, re-filling the dirty liquid in the distillation tank 1, and then restarting distillation to start the next concentration period.
The pollution degree in the distillation tank 1 is judged according to the length of the concentration period, the concentration tank B3 can be started when the pollution degree is serious, and a new concentration tank can be additionally arranged according to the situation.
The vapors generated by the distillation of the two tanks A2 and B3 are fed to the distillation tank 1 and pumped out together.
Boiling the dirty liquid in the concentration tank to finish a first concentration period, replenishing the dirty liquid in the distillation tank into the concentration tank again, restarting distillation, finishing the 2 nd concentration period until the n concentration period, setting a threshold value of n, and stopping feeding the liquid into the concentration tank from the distillation tank when the n is greater than the threshold value of n, wherein the liquid in the distillation tank is clean.
The actual run time threshold t and the threshold n may be set based on whether it is in conjunction with liquid sample detection.
Finally, it should be noted that: the foregoing description is only a preferred embodiment of the present application, and the present application is not limited thereto, but it is to be understood that modifications and equivalents of some of the technical features described in the foregoing embodiments may be made by those skilled in the art, although the present application has been described in detail with reference to the foregoing embodiments. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the protection scope of the present application.
Claims (3)
1. A dynamic concentration distillation method, comprising the steps of:
s1, communicating at least one concentration tank on a distillation tank through a pipeline with a valve; after the distillation tank continuously distills for a period of time, part of the sewage in the distillation tank is led into the concentration tank;
s2, boiling the dirty liquid in a concentration tank to finish a first concentration period, supplementing the dirty liquid in a distillation tank into the concentration tank again, and restarting distillation to finish a2 nd concentration period;
s3, by the pushing, finishing the nth concentration period, setting a threshold value of n, and when n is greater than the threshold value n When the distillation tank is clean, stopping feeding liquid from the distillation tank to the concentration tank, and returning to the step S1 after the distillation tank continuously runs for a period of time;
s4, setting the total liquid amount in the concentrating tank to be V2 and the liquid amount to be fed to the feeding stop to be V1 when the concentrating tank starts to feed liquid, wherein the distillation amount at each time is DeltaV=V1-V2; the distillation time required from the distillation of the V1 position to the distillation of the V2 position is deltat, the threshold value of deltat is set, and when deltat is more than or equal to the threshold value t In this case, the liquid in the concentration tank A2 is completely discharged, and the contaminated liquid in the distillation tank is refilled into the concentration tank and distillation is restarted.
2. The dynamic concentration distillation method as claimed in claim 1, wherein the pollution level of the distillation tank is determined according to the length of the concentration period, and when the pollution level is serious, a new concentration tank is additionally arranged, and the concentration of the sewage is performed at the same time;
when Δtn < Δtx, light contamination is represented; delta tn is greater than or equal to delta tx, and represents heavy oil stain; wherein Deltatn is the time taken for DeltaVn to distill off; Δtx is the distillation time corresponding to the optimal equilibrium point.
3. The dynamic concentrating and distilling method according to claim 1, wherein the liquid in the distillation tank is introduced into the concentrating tank through a valve by applying negative pressure to the concentrating tank to cause a pressure difference between the distillation tank and the concentrating tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210180651.8A CN115025506B (en) | 2022-02-26 | 2022-02-26 | Dynamic concentration distillation method of distillation recovery system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210180651.8A CN115025506B (en) | 2022-02-26 | 2022-02-26 | Dynamic concentration distillation method of distillation recovery system |
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| Publication Number | Publication Date |
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| CN115025506A CN115025506A (en) | 2022-09-09 |
| CN115025506B true CN115025506B (en) | 2023-11-10 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10324105A1 (en) * | 2003-05-27 | 2004-12-23 | Dr. O.K. Wack Chemie Gmbh | Method and device for liquid cleaning of objects |
| CN109771979A (en) * | 2019-02-15 | 2019-05-21 | 江苏金色工业炉股份有限公司 | A kind of novel hydrocarbon cleaning machine Distallation systm |
| CN210583713U (en) * | 2019-07-09 | 2020-05-22 | 福建华佳彩有限公司 | Recovery unit of washing liquid |
| CN213103580U (en) * | 2020-09-04 | 2021-05-04 | 苏州德韬科技有限公司 | Hydrocarbon distillation recovery unit |
-
2022
- 2022-02-26 CN CN202210180651.8A patent/CN115025506B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10324105A1 (en) * | 2003-05-27 | 2004-12-23 | Dr. O.K. Wack Chemie Gmbh | Method and device for liquid cleaning of objects |
| CN109771979A (en) * | 2019-02-15 | 2019-05-21 | 江苏金色工业炉股份有限公司 | A kind of novel hydrocarbon cleaning machine Distallation systm |
| CN210583713U (en) * | 2019-07-09 | 2020-05-22 | 福建华佳彩有限公司 | Recovery unit of washing liquid |
| CN213103580U (en) * | 2020-09-04 | 2021-05-04 | 苏州德韬科技有限公司 | Hydrocarbon distillation recovery unit |
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| CN115025506A (en) | 2022-09-09 |
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