CN1486770A - Directly cooling solvent recovering method and system - Google Patents
Directly cooling solvent recovering method and system Download PDFInfo
- Publication number
- CN1486770A CN1486770A CNA021355894A CN02135589A CN1486770A CN 1486770 A CN1486770 A CN 1486770A CN A021355894 A CNA021355894 A CN A021355894A CN 02135589 A CN02135589 A CN 02135589A CN 1486770 A CN1486770 A CN 1486770A
- Authority
- CN
- China
- Prior art keywords
- refrigerant
- solvent
- cooling
- knockout drum
- water knockout
- 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
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention relates to directly cooling solvent recovering method and system. Solvent vapor from steaming, stoving and evaporating system is led directly to directly cooling condensator, where solvent vapor contacts directly with refrigerant for condensation via heat exchang; the condensed liquid is made to enter the water separator for separating the refrigerant and the solvent; produced tail gas is made to enter the tail gas recovering system; solvent separated in the water separator is solvent pump pumped for reuse and the refrigerant is made to enter the cooling tower for reuse. The present invention has high solvent recovering efficiency, low investment in equipment, less covered area, no scale in the condensator with long service life.
Description
Technical field
The present invention relates to leach the method for recovering solvents in the oily process of system, relate to the system that reclaims solvent simultaneously.
Technical background
Since leaching oil-producing technique invention use, the solvent recycling is the important step of this technology always.Factors such as its investment, manufacturing, service life are perplexing engineers and technicians and investment and production producer always.Solvent recovery is to utilize solvent vapo(u)r to meet cold and condensation, cooling, more further the turnout reason to reach recycling purpose.At present solvent vapo(u)r condensation, cooling processing are generally adopted partition type condenser condenses, cooling, though the condenser kind has a lot, as carbon steel pipe bundle condenser, stainless steel pipe bundle condenser, aluminium alloy pipe bundle condenser, plate-type condenser etc., but all exist following shortcoming: 1, manufacturing expense height: above-mentioned condenser Master Cost and manufacturing expense are all higher, particularly plate-type condenser needs special dies, and manufacture difficulty and expense are high always.2, heat-transfer effect is poor: with partition type condenser condenses, when solvent recovery is carried out in cooling, the heat of solvent vapo(u)r must pass through condensate liquid, metal level, layer of scale, the formed thermal resistance of refrigerant detention layer, just can pass to refrigerant, hot and cold two kinds of thermophore temperature difference must be more than 20 ℃, otherwise can not reach heat-transfer effect well.3, fouling easily, the life-span is short: owing to exist two kinds of thermophore temperature difference and detention layer in diabatic process, make Ca2+, Mg2+ fouling on metallic walls in the refrigerant detention layer, influence heat-transfer effect.Simultaneously the equipment of carbon steel, aluminum alloy material also exist easily be corroded, the equal problem of thermal coefficient of expansion, make that the dirt layer is thicker and reduce the life-span.4, equipment is many with quantity, floor space is big: in traditional solvent recovery process, the solvent vapo(u)r of deriving from equipment such as infuser, evapo-separated machine, evaporimeter, strippers need enter different condensers and carry out condensation, therefore need nearly six condenser of configuration, this must increase the investment of floor space and equipment, factory building.5, maintenance difficulty: because complex structures such as pipe bundle condenser, plate-type condensers, dismounting is inconvenient, thereby has caused the difficulty of maintenance aspects such as cleaning dirt and sealing.
Summary of the invention
The purpose of this invention is to provide a kind of directly cooling solvent recovering method.The present invention also aims to provide a kind of solvent recovering system of realizing said method.
For achieving the above object, the technical solution used in the present invention is: directly cooling solvent recovering method, to feed the direct-cooling condensation device from the solvent vapo(u)r that steams baking, vapo(u)rization system and directly contact the generation heat exchange and condensation with refrigerant, tail gas enters exhaust gas recovery system, condensate liquid enters water knockout drum, make refrigerant and separated from solvent, the solvent that water knockout drum is told is extracted out through solvent pump and is reused, and refrigerant is reused after entering the cooling tower cooling.
The refrigerant of telling from water knockout drum enters and makes it to enter negative pressure precipitation tower before the cooling tower cooling and remove wherein residual solvent.
Described direct-cooling condensation device is two, and the residual solvent steam that produces after the last condenser condenses feeds the further condensation of back one condenser.
The direct-cooling type solvent recovering system of realizing said method comprises at least one direct-cooling condensation device, the refrigerant import of condenser links to each other with the refrigerant circulatory pool by pipeline, the condensate outlet of condenser links to each other with water knockout drum, on the pipeline that links to each other between water knockout drum and the refrigerant cooling tower refrigerant pump is arranged, the control corresponding valve all is housed on each pipeline.
Between water knockout drum and refrigerant cooling tower, be provided with negative pressure precipitation device, the import of negative pressure precipitation device links to each other by pipeline with the refrigerant exit of water knockout drum, its outlet is connected with the refrigerant cooling tower by the refrigerant surge tank, and the gas vent of negative pressure precipitation device links to each other with the solvent vapo(u)r import of direct-cooling condensation device with pipeline by vavuum pump.
The tail gas outlet of condenser is connected with the tail gas water knockout drum by pipeline, and the condensate outlet of tail gas water knockout drum is connected with water knockout drum.
Described direct-cooling condensation device is that the tank body of filler or the tank body that spray head is equipped with at the top are housed.Described filler is a ripple packing.
Adopt such scheme to make the present invention have following good effect:
1, manufacturing expense is low: direct-cooling condensation device of the present invention does not need a wall construction, can adopt the manufacturing of ordinary carbon steel material, and simple in structure, easily manufactured, expense is low.
2, heat-transfer effect is good: in the present invention, solvent by steam in the phase transition process of liquid, its process is: solvent vapo(u)r → solvent vapo(u)r mixes with refrigerant → and solvent condenses liquid, refrigerant mixture, two kinds of heat transport fluids are directly mixed, do not have the partition heat transfer process, thereby eliminated thermal resistance such as detention layer and fouling factor in the heat transfer process, as long as refrigerant temperature is no more than 60 ℃, certainly temperature is low more good more, as long as refrigerant does not freeze.
3, non-scaling, long service life: because the condensation of solvent vapo(u)r is directly to mix to carry out on the filling surface of direct-cooling condensation device, so there are not processes such as heat conductive wall fouling and the conduction of partition heat, simultaneously, inner tank wall can be coated with anti-corrosion resin to prolong its life-span.
4, equipment is few with quantity, and floor space is little: in the present invention, the configuration quantity of condenser obviously reduces, and floor space is little.According to production scale, condenser can also can be two or more only with one.
5, maintenance is easily: because the direct-cooling condensation device is simple in structure, and convenient disassembly.Thereby maintenance aspect ratios such as cleaning dirt and sealing are easier to.Simultaneously, in reclaiming dissolving agent process, only need control refrigerant temperature and flow to get final product, very convenient, stable.
Description of drawings
Accompanying drawing is depicted as the schematic diagram of direct-cooling type solvent recovering system of the present invention;
The specific embodiment
In this direct-cooling type solvent recovering system, condenser comprises the first direct-cooling condensation device L-06 and the second direct-cooling condensation device L-07, the refrigerant import of two condensers all links to each other with refrigerant circulatory pool L-05 by pipeline, pump, the condensate outlet of two condensers all links to each other with water knockout drum L-01, and the gas vent of the first direct-cooling condensation device L-06 links to each other by pipeline with the solvent vapo(u)r import of the second condenser L-07.Between water knockout drum L-01 and refrigerant cooling tower L-04, be provided with negative pressure precipitation device L-02, negative pressure precipitation device L-02 import links to each other by pipeline with water knockout drum L-01, its outlet is connected by refrigerant surge tank L-03 with refrigerant cooling tower L-04, and the solvent vapo(u)r import with the second direct-cooling condensation device L-07 links to each other the gas vent of negative pressure precipitation device L-02 with pipeline by vavuum pump B-05.Be provided with tail gas water knockout drum L-08 on the gas vent of the second direct-cooling condensation device L-07 and pipeline that exhaust gas recovery system links to each other, the condensate outlet of this tail gas water knockout drum L-08 links to each other by pipeline with water knockout drum L-01.On the pipeline that links to each other between water knockout drum and the negative pressure precipitation device refrigerant drawing pump B-02 is housed, on the pipeline that links to each other between refrigerant surge tank and the refrigerant cooling tower refrigerant pump B-03 is arranged, on the pipeline that links to each other between refrigerant circulatory pool L-05 and the first direct-cooling condensation device and the second direct-cooling condensation device refrigerant pump B-04 is arranged, the control corresponding valve all is housed on each pipeline.
The direct-cooling condensation device that the present invention adopts can be the tank body of interior filling material, and filler can adopt ripple packing, the filler that also can adopt other to be fit to.Certainly, the direct-cooling condensation device also can adopt other structures, can be the spray head of refrigerant atomisation as loading onto at the tank body internal upper part.In the present invention, carry out heat exchange, do not need by partition type condensation structure, so condenser is called the direct-cooling condensation device because directly contact between refrigerant and the solvent vapo(u)r.Negative pressure precipitation device is to utilize vavuum pump that it is evacuated, so that remove a small amount of solvent steam that contains from the refrigerant that water knockout drum is extracted out, it can be a slack tank body, also an amount of filler can be housed therein.Direct-cooling condensation device and negative pressure precipitation device no longer illustrate.
In production scale hour, also can only adopt a direct-cooling condensation device, save the second direct-cooling condensation device.When production scale is big, also can increase the quantity of direct-cooling condensation device according to actual needs.
It is as follows to adopt above-mentioned solvent recovering system to carry out the method for solvent recovery:
Enter the first direct-cooling condensation device L-06 from the solvent vapo(u)r that steams baking, vapo(u)rization system and directly contact the generation heat exchange and condensation with refrigerant, condensate liquid enters water knockout drum L-01, makes refrigerant and separated from solvent; The free gas that contains a small amount of solvent steam enters the second direct-cooling condensation device L-07 with the solvent vapo(u)r from infuser and directly contacts the generation heat exchange and condensation with refrigerant, and condensate liquid enters water knockout drum L-01, makes refrigerant and separated from solvent.The free gas that contains solvent vapo(u)r on a small quantity that the second direct-cooling condensation device L-07 discharges enters tail gas water knockout drum L-08 and divides water, and refrigerant enters water knockout drum L-01, and gas enters exhaust gas recovery system.The solvent that water knockout drum L-01 tells is extracted out by solvent pump B-01 and is reused.And refrigerant enters negative pressure precipitation tower L-02 and removes wherein residual solvent, and solvent vapo(u)r enters the second direct-cooling condensation device L-07 condensation, and refrigerant is reused after entering refrigerant cooling tower L-04 cooling.The employing of the second direct-cooling condensation device can reduce the load of the first direct-cooling condensation device on the one hand, and the negative pressure that more helps infuser on the other hand produces.
Claims (8)
1, a kind of directly cooling solvent recovering method, it is characterized in that, to feed the direct-cooling condensation device from the solvent vapo(u)r that steams baking, vapo(u)rization system and directly contact the generation heat exchange and condensation with refrigerant, tail gas enters exhaust gas recovery system, condensate liquid enters water knockout drum, make refrigerant and separated from solvent, the solvent that water knockout drum is told is extracted out through solvent pump and is reused, and refrigerant is reused after entering the cooling tower cooling.
2, the method for claim 1 is characterized in that, the refrigerant of telling from water knockout drum enters and makes it to enter negative pressure precipitation tower before the cooling tower cooling and remove wherein residual solvent.
3, the method for claim 1 is characterized in that, described direct-cooling condensation device is two, and the residual solvent steam that produces after the last condenser condenses feeds the further condensation of back one condenser.
4, a kind of direct-cooling type solvent recovering system of realizing claim 1,2 or 3 described methods, it is characterized in that, comprise at least one direct-cooling condensation device, the refrigerant import of condenser links to each other with the refrigerant circulatory pool by pipeline, the condensate outlet of condenser links to each other with water knockout drum, on the pipeline that links to each other between water knockout drum and the refrigerant cooling tower refrigerant pump is arranged, the control corresponding valve all is housed on each pipeline.
5, system as claimed in claim 4, it is characterized in that, between water knockout drum and refrigerant cooling tower, be provided with negative pressure precipitation device, the import of negative pressure precipitation device links to each other by pipeline with the refrigerant exit of water knockout drum, its outlet is connected with the refrigerant cooling tower by the refrigerant surge tank, and the gas vent of negative pressure precipitation device links to each other with the solvent vapo(u)r import of direct-cooling condensation device with pipeline by vavuum pump.
As claim 4 or 5 described systems, it is characterized in that 6, the tail gas outlet of condenser is connected with the tail gas water knockout drum by pipeline, the condensate outlet of tail gas water knockout drum is connected with water knockout drum.
As claim 4 or 5 described systems, it is characterized in that 7, described direct-cooling condensation device is that the tank body of filler or the tank body that spray head is equipped with at the top are housed.
8, system as claimed in claim 7 is characterized in that, described filler is a ripple packing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02135589 CN1225298C (en) | 2002-09-30 | 2002-09-30 | Directly cooling solvent recovering method and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02135589 CN1225298C (en) | 2002-09-30 | 2002-09-30 | Directly cooling solvent recovering method and system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1486770A true CN1486770A (en) | 2004-04-07 |
| CN1225298C CN1225298C (en) | 2005-11-02 |
Family
ID=34146213
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02135589 Expired - Fee Related CN1225298C (en) | 2002-09-30 | 2002-09-30 | Directly cooling solvent recovering method and system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1225298C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102836565A (en) * | 2012-09-12 | 2012-12-26 | 河北工业大学 | Vacuum system solvent recovering method and device |
| CN103463832A (en) * | 2013-10-09 | 2013-12-25 | 吉首大学 | Tail gas refrigeration recycling processing device |
| CN104536364A (en) * | 2014-12-03 | 2015-04-22 | 武汉旭日华科技发展有限公司 | Organic solvent recovery device with air inlet control and control method thereof |
-
2002
- 2002-09-30 CN CN 02135589 patent/CN1225298C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102836565A (en) * | 2012-09-12 | 2012-12-26 | 河北工业大学 | Vacuum system solvent recovering method and device |
| CN103463832A (en) * | 2013-10-09 | 2013-12-25 | 吉首大学 | Tail gas refrigeration recycling processing device |
| CN104536364A (en) * | 2014-12-03 | 2015-04-22 | 武汉旭日华科技发展有限公司 | Organic solvent recovery device with air inlet control and control method thereof |
| CN104536364B (en) * | 2014-12-03 | 2017-05-10 | 武汉旭日华科技发展有限公司 | Organic solvent recovery system with air inlet control and control method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1225298C (en) | 2005-11-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101063595A (en) | SCAL indirect air cooling system | |
| CN101831348B (en) | Method for separating and recovering product oil from waste lubricating oil and device thereof | |
| CN1975311A (en) | Liquid separating air condenser | |
| CN1131171C (en) | Equipment for recovering and utilizing heat energy generated by phosphor combustion and system for preparing phosphoric acid by hot method | |
| CN1225298C (en) | Directly cooling solvent recovering method and system | |
| CN113828121B (en) | Methyl chloride recovery system and method | |
| CN102267868A (en) | Industrial production apparatus for trichloroethylene | |
| CN101423247A (en) | Method for removing vanadium impurity in titanic chloride by forced assisted-circulation heating | |
| CN2872269Y (en) | Improved equal flow-speed gas-liquid heat exchanger | |
| CN2863760Y (en) | Apparatus for preparation liquid sulfur trioxide from oleum | |
| CN112274960A (en) | Foam type rectifying tower and using method thereof | |
| CN210215250U (en) | High-efficient distillation system of coal tar | |
| CN209161961U (en) | A kind of purification-recovery system for damaged tire cracking oil gas | |
| CN201762266U (en) | Trichloroethylene industrialized production device | |
| CN2436475Y (en) | Gas discharge recovery device for oil and gas tank | |
| CN216712015U (en) | Circulating system for recycling waste heat of ammonia water for potassium carbonate desulfurization regeneration heat source | |
| CN215411417U (en) | Multi-stage horizontal gas drainer | |
| CN103602319B (en) | Conduction oil light component system for separating and purifying | |
| CN209508152U (en) | A kind of material filling type coke tar distillation tower | |
| CN107246815A (en) | A kind of anti-corrosion heat-condutive oil heat exchanger | |
| CN1065718A (en) | Steam heat supply closed circulation equipment | |
| CN1039574C (en) | Multi-cell heating system | |
| CN2415821Y (en) | Eddy degassing liquid | |
| CN217549322U (en) | Device for improving oil mist separation | |
| CN109355082B (en) | Packing type tar distillation tower |
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 | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |