CN104353258B - Subtract top pumped vacuum systems and technique - Google Patents
Subtract top pumped vacuum systems and technique Download PDFInfo
- Publication number
- CN104353258B CN104353258B CN201410658242.XA CN201410658242A CN104353258B CN 104353258 B CN104353258 B CN 104353258B CN 201410658242 A CN201410658242 A CN 201410658242A CN 104353258 B CN104353258 B CN 104353258B
- Authority
- CN
- China
- Prior art keywords
- condenser
- pump
- liquid
- heating agent
- connects
- 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.)
- Active
Links
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention relates to one and subtract top pumped vacuum systems and technique, what comprise connection vacuum tower subtracts top gas pipeline, subtract top gas pipeline described in it is characterized in that to connect the first condenser successively, cross the first vacuum pumping pump, the second condenser, the second vacuum pumping pump and liquid-ring vacuum pump, the heat transferring medium of the first condenser and the second condenser is from absorber, and described absorber connects evaporimeter and refrigerant tank, heating agent tank.Provided by the present invention subtract top pumped vacuum systems and technique water saving, good energy-conserving effect, stable and reliable operation, substantially increases the economic benefit of device.
Description
Technical field
The present invention relates to chemical plant installations, specifically refer to that one subtracts top pumped vacuum systems and technique.
Background technology
Atmospheric and vacuum distillation unit is the faucet device of oil-processing enterprises, the design of this device, the level of production directly have influence on the economic benefit of full factory, and to subtract top pumped vacuum systems be one of key components of this device, closely related with the investment of device, extracting rate, product quality, energy consumption.The effect of Top of Vacuum Tower pumped vacuum systems is taken away continuously by the oil gas of Top of Vacuum Tower, to ensure the vacuum level requirements of vacuum tower.
Usually adopt multistage steam evacuation to combinationally use in prior art, need after vacuum jet to be equipped with condenser.The method have simple and compact for structure, movement-less part, processing cost are low, simple to operate and safeguard the advantages such as less, but its efficiency is lower, and the steam after vacuumizing enter system after add condensing cooling load, energy consumption is high.
Summary of the invention
Technical problem to be solved by this invention be provide a kind of operating efficiency high for the present situation of prior art and energy consumption low subtract top pumped vacuum systems.
Another technical problem to be solved by this invention be to provide the high and energy consumption of a kind of operating efficiency low subtract top evacuation process.
The present invention solves the problems of the technologies described above adopted technical scheme: this subtracts top pumped vacuum systems, what comprise connection vacuum tower subtracts top gas pipeline, the first passage that top gas pipeline connects the first condenser is subtracted described in it is characterized in that, the gaseous phase outlet of the first condenser first passage connects the first passage of the second condenser by the first vacuum pumping pump, the liquid-phase outlet connection of the first condenser first passage subtracts top water distributing can; The described gaseous phase outlet subtracting top water distributing can connects discharge line, and the liquid-phase outlet subtracting top water distributing can connects upstream device by sewage pump, and the oil phase outlet subtracting top water distributing can connects upstream device by sump (waste oil) pump;
The gaseous phase outlet of described second condenser first passage passes through the gas phase entrance of the second vacuum pumping pump connecting fluid ring vacuum pump, and the liquid-phase outlet of the second condenser first passage connects the liquid phase entrance of described liquid-ring vacuum pump;
The gaseous phase outlet of described liquid-ring vacuum pump connects upstream device by described discharge line; The liquid-phase outlet of described liquid-ring vacuum pump subtracts top water distributing can entrance described in the first pump connection;
The outlet of refrigerant tank connects the refrigerant inlet of absorber by the second pump, the refrigerant exit of described absorber is connected the second channel of described first condenser by the first pipeline, connected the second channel of the second condenser by second pipe; The second channel of described first condenser is connected the entrance of described refrigerant tank with the second channel of described second condenser;
The heating agent entrance of described absorber connects the heating agent outlet of evaporimeter, and the heating agent entrance of described evaporimeter is connected the outlet of heating agent tank by heat exchanger and the 3rd pump, and the heating agent outlet of described absorber connects the entrance of described heating agent tank.
Preferably, described first vacuum pumping pump and described second vacuum pumping pump are Roots vaccum pump.
Use above-mentioned subtract top pumped vacuum systems subtract top evacuation process, it is characterized in that comprising the steps:
The top gas that subtracts that temperature is 60-70 DEG C, pressure is 2-3KPa enters in the first condenser by subtracting top gas pipeline, be that first burst of refrigerant heat exchange of 6-10 DEG C is to after 10-20 DEG C with the temperature from absorber, being compressed into temperature by the first vacuum pumping pump is that the air-flow of 70-75 DEG C enters condensation in the second condenser, with the temperature from absorber be second burst of refrigerant heat exchange of 6-10 DEG C to 15-20 DEG C, then detach via the second vacuum pumping pump and liquid-ring vacuum pump successively and send to upstream device;
The liquid phase that described first condenser condenses is got off enters and subtracts in the water distributing can of top, the liquid phase come by the first pumping with the liquid-phase outlet of described liquid-ring vacuum pump together subtract push up in water distributing can carry out oil, gas, water is separated, oil after separation is sent by sump (waste oil) pump, isolated water is sent by sewage pump, and isolated gas is incorporated to discharge line;
Temperature in refrigerant tank is that the refrigerant of 10-15 DEG C enters in absorber by the second pump, is divided into two strands after being cooled to 6-10 DEG C, wherein first strand send to the first condenser with subtract top gas heat exchange, second strand send to the second condenser with compression after subtract top gas heat exchange; Described first strand is 7-9:1 with the flow-rate ratio of second strand; Two strands of refrigerants after heat exchange return refrigerant tank Inner eycle and use;
Temperature from heating agent tank is that first the heating agent of 110-120 DEG C enters in evaporimeter, is cooled to 75-85 DEG C, delivers to heat exchange in absorber and return heating agent tank after 60-70 DEG C from deaerated water heat absorption out-of-bounds after there is steam.
Preferably, described refrigerant is lithium bromide, and described heating agent is hot water.
Compared with prior art, provided by the present invention subtract top pumped vacuum systems and technique water saving, good energy-conserving effect, stable and reliable operation, substantially increases the economic benefit of device.Be used in certain 800,000 tons/year of pitch lube plant project, subtract top pumped vacuum systems compared to routine, device saves 1.0MPa steam 2.1 ten thousand tons/year, recirculated water 3,900,000 tons/year, reduce the discharge capacity 2.1 ten thousand tons/year of oil-polluted water, energy-conservation more than 65%, economic benefit is fairly obvious.
Accompanying drawing explanation
Fig. 1 is embodiment of the present invention schematic diagram.
Detailed description of the invention
Below in conjunction with accompanying drawing embodiment, the present invention is described in further detail.
As shown in Figure 1, this subtract top pumped vacuum systems comprise:
What connect vacuum tower subtracts top gas pipeline 1, subtract the first passage that top gas pipeline 1 connects the first condenser 2, the gaseous phase outlet of the first condenser 2 first passage connects the first passage of the second condenser 4 by the first Roots vaccum pump 3, the liquid-phase outlet connection of the first condenser 2 first passage subtracts top water distributing can 8; The described gaseous phase outlet subtracting top water distributing can 8 connects discharge line 7, and the liquid-phase outlet subtracting top water distributing can 8 connects upstream device by sewage pump 14, and the oil phase outlet subtracting top water distributing can connects upstream device by sump (waste oil) pump 15;
The gaseous phase outlet of described second condenser 4 first passage passes through the gas phase entrance of the second Roots vaccum pump 5 connecting fluid ring vacuum pump 6, and the liquid-phase outlet of the second condenser 4 first passage connects the liquid phase entrance of described liquid-ring vacuum pump 6;
The gaseous phase outlet of described liquid-ring vacuum pump 6 connects upstream device by described discharge line 7; Top water distributing can entrance is subtracted described in the liquid-phase outlet of described liquid-ring vacuum pump is connected by the first pump 19;
The outlet of refrigerant tank 12 connects the refrigerant inlet of absorber 10 by the second pump 13, the refrigerant exit of described absorber 10 is connected the second channel of described first condenser 2 by the first pipeline 17, connected the second channel of the second condenser 4 by second pipe 18; The second channel of described first condenser is connected the entrance of described refrigerant tank with the second channel of described second condenser; The refrigerant stored in refrigerant tank in the present embodiment is lithium bromide.
The heating agent entrance of described absorber 10 connects the heating agent outlet of evaporimeter 9, and the heating agent entrance of described evaporimeter is connected the outlet of heating agent tank 11 successively with the 3rd pump 20 by heat exchanger 16, and the heating agent outlet of described absorber 10 connects the entrance of described heating agent tank 11.Heating agent stored in heating agent tank in the present embodiment is hot water.
The above-mentioned top evacuation process that subtracts subtracting top pumped vacuum systems is used to comprise the steps:
The top gas that subtracts that temperature from atmospheric and vacuum distillation unit (not shown) is 65 DEG C, pressure is 2.67KPa enters in the first condenser 2 by subtracting top gas pipeline 1, after being first burst of refrigerant heat exchange to 15 DEG C of 8 DEG C with the temperature from absorber, being compressed into temperature by the first Roots vaccum pump 3 is that the air-flow of 72.65 DEG C enters condensation in the second condenser 4, with second burst of refrigerant heat exchange to 17 DEG C that the temperature from absorber is 8 DEG C, then detach via the second Roots vaccum pump 5 and liquid-ring vacuum pump 6 successively and send to upstream device;
The temperature that described first condenser 2 condensation is got off be 40 DEG C of liquid phases enter subtract top water distributing can 8 in, with the liquid-phase outlet of described liquid-ring vacuum pump 6 by the temperature that the first pumping comes be 65 DEG C of liquid phases together subtract push up in water distributing can 8 carry out oil, gas, water is separated, oil after separation is sent by sump (waste oil) pump 15, isolated water is sent by sewage pump 14, and isolated gas is incorporated to discharge line 7;
Temperature in refrigerant tank 12 is that the refrigerant of 13 DEG C is entered in absorber 10 by the second pump 13, is divided into two strands after being cooled to 8 DEG C, wherein first strand send to the first condenser with subtract top gas heat exchange, second strand send to the second condenser with compression after subtract top gas heat exchange; Described first strand is 9:1 with the flow-rate ratio of second strand; Temperature after heat exchange is that 13 DEG C of two strands of refrigerants return the use of refrigerant tank 12 Inner eycle;
Temperature from heating agent tank 11 is that first the heating agent of 65 DEG C enters heat exchange to 115 DEG C in heat exchanger 16, then enter in evaporimeter 9, occur to be cooled to 80.5 DEG C after steam from deaerated water heat absorption out-of-bounds, after delivering in absorber 10 heat exchange to 65 DEG C, return heating agent tank 11.
This is subtracted top pumped vacuum systems to support the use at 800,000 tons/year of pitch lube plants " in the design of project; subtract top pumped vacuum systems compared to routine; can save 1.0MPa steam 2.1 ten thousand tons/year; save recirculated water 3,900,000 tons/year; oil-polluted water discharge capacity reduces 2.1 ten thousand tons/year; although power consumption is by increase by 1,680,000 kwh/, but subtract top pumped vacuum systems and can save energy more than 65% generally, economic benefit is fairly obvious.And the higher condensers at different levels of Investment portion are because have employed the chilled water of-8 DEG C as after cooling medium, and its specification of equipment obviously diminishes, although therefore equipment adds, the entirety investment subtracting top pumped vacuum systems does not increase.
Claims (4)
1. one kind subtracts top pumped vacuum systems, what comprise connection vacuum tower subtracts top gas pipeline (1), the first passage that top gas pipeline (1) connects the first condenser (2) is subtracted described in it is characterized in that, the gaseous phase outlet of the first condenser (2) first passage connects the first passage of the second condenser (4) by the first vacuum pumping pump (3), the liquid-phase outlet connection of the first condenser (2) first passage subtracts top water distributing can (8); The described gaseous phase outlet subtracting top water distributing can (8) connects discharge line (7), the liquid-phase outlet subtracting top water distributing can (8) connects upstream device by sewage pump (14), and the oil phase outlet subtracting top water distributing can connects upstream device by sump (waste oil) pump (15);
The gaseous phase outlet of described second condenser (4) first passage passes through the gas phase entrance of the second vacuum pumping pump (5) connecting fluid ring vacuum pump (6), and the liquid-phase outlet of the second condenser (4) first passage connects the liquid phase entrance of described liquid-ring vacuum pump (6);
The gaseous phase outlet of described liquid-ring vacuum pump (6) connects upstream device by described discharge line (7); The liquid-phase outlet of described liquid-ring vacuum pump subtracts top water distributing can entrance by described in the first pump (19) connection;
The outlet of refrigerant tank (12) connects the refrigerant inlet of absorber (10) by the second pump (13), the refrigerant exit of described absorber (10) is connected the second channel of described first condenser (2) by the first pipeline (17), connected the second channel of the second condenser (4) by second pipe (18); The second channel of described first condenser is connected the entrance of described refrigerant tank with the second channel of described second condenser;
The heating agent entrance of described absorber (10) connects the heating agent outlet of evaporimeter (9), the heating agent entrance of described evaporimeter is connected the outlet of heating agent tank (11) with the 3rd pump (20) by heat exchanger (16), the heating agent outlet of described absorber (10) connects the entrance of described heating agent tank (11).
2. according to claim 1ly subtract top pumped vacuum systems, it is characterized in that described first vacuum pumping pump (3) and described second vacuum pumping pump are Roots vaccum pump.
3. use subtract as claimed in claim 1 top pumped vacuum systems subtract top evacuation process, it is characterized in that comprising the steps:
The top gas that subtracts that temperature is 60-70 DEG C, pressure is 2-3KPa enters in the first condenser (2) by subtracting top gas pipeline (1), be that first burst of refrigerant heat exchange of 6-10 DEG C is to after 10-20 DEG C with the temperature from absorber, being compressed into temperature by the first vacuum pumping pump (3) is that the air-flow of 70-75 DEG C enters the second condenser (4) interior condensation, with the temperature from absorber be second burst of refrigerant heat exchange of 6-10 DEG C to 15-20 DEG C, then detach via the second vacuum pumping pump (5) and liquid-ring vacuum pump (6) successively and send to upstream device;
The liquid phase that the condensation of described first condenser (2) is got off enters and subtracts in top water distributing can (8), the liquid phase come by the first pumping with the liquid-phase outlet of described liquid-ring vacuum pump (6) together subtract push up in water distributing can (8) carry out oil, gas, water is separated, oil after separation is sent by sump (waste oil) pump (15), isolated water is sent by sewage pump (14), and isolated gas is incorporated to discharge line (7);
Temperature in refrigerant tank (12) is that the refrigerant of 10-15 DEG C enters in absorber (10) by the second pump (13), two strands are divided into after being cooled to 6-10 DEG C, wherein first strand send to the first condenser with subtract top gas heat exchange, second strand send to the second condenser with compression after subtract top gas heat exchange; Described first strand is 7-9:1 with the flow-rate ratio of second strand; Two strands of refrigerants after heat exchange return refrigerant tank (12) Inner eycle and use;
Temperature from heating agent tank (11) is that first the heating agent of 110-120 DEG C enters in evaporimeter (9), be cooled to 75-85 DEG C after there is steam from deaerated water heat absorption out-of-bounds, deliver to absorber (10) interior heat exchange and return heating agent tank (11) after 60-70 DEG C.
4. according to claim 3ly subtract top evacuation process, it is characterized in that described refrigerant is lithium bromide, described heating agent is hot water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410658242.XA CN104353258B (en) | 2014-11-18 | 2014-11-18 | Subtract top pumped vacuum systems and technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410658242.XA CN104353258B (en) | 2014-11-18 | 2014-11-18 | Subtract top pumped vacuum systems and technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104353258A CN104353258A (en) | 2015-02-18 |
| CN104353258B true CN104353258B (en) | 2016-01-06 |
Family
ID=52520620
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410658242.XA Active CN104353258B (en) | 2014-11-18 | 2014-11-18 | Subtract top pumped vacuum systems and technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104353258B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10016721B1 (en) | 2017-05-25 | 2018-07-10 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desufurization process and apparatus |
| US10092877B1 (en) | 2017-05-25 | 2018-10-09 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10099170B1 (en) | 2017-06-14 | 2018-10-16 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US10112145B1 (en) | 2017-09-07 | 2018-10-30 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
| US20190001267A1 (en) | 2017-07-03 | 2019-01-03 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10207220B2 (en) | 2017-03-15 | 2019-02-19 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for removing sulfur oxides from gas |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9370745B2 (en) | 2013-04-24 | 2016-06-21 | Jiangsu New Century Jiangnan Environmental Protection Co., Ltd | Flue gas-treating method and apparatus for treating acidic tail gas by using ammonia process |
| CN105238436A (en) * | 2015-08-25 | 2016-01-13 | 海南汉地阳光石油化工有限公司 | Decompression vacuum extraction system, decompression system, and method for extracting agricultural lubricating oil |
| CN116510513A (en) | 2018-04-13 | 2023-08-01 | 江苏新世纪江南环保股份有限公司 | Oxidation method and device for ammonia desulfurization solution |
| CN110732227B (en) | 2018-07-20 | 2023-02-21 | 江南环保集团股份有限公司 | Method and device for treating acid gas |
| CN111957183A (en) | 2019-12-26 | 2020-11-20 | 江苏新世纪江南环保股份有限公司 | Improved ammonia desulphurization method for controlling aerosol generation in absorption process |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2325207C1 (en) * | 2007-01-31 | 2008-05-27 | Валерий Григорьевич Цегельский | Device for vacuum distillation of raw predominantly petroleum raw |
| CN201692678U (en) * | 2010-03-18 | 2011-01-05 | 南京蓝星化工新材料有限公司 | Vacuum system |
| CN204319802U (en) * | 2014-11-18 | 2015-05-13 | 镇海石化工程股份有限公司 | Subtract top pumped vacuum systems |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0631103A (en) * | 1992-07-18 | 1994-02-08 | Marusan Shokai:Kk | Vacuum distillation method of combustible solvent for work washing and vacuum distillation apparatus |
| JP4715765B2 (en) * | 2007-02-09 | 2011-07-06 | 株式会社日立プラントテクノロジー | Liquid concentrating system and liquid concentrator used therefor |
-
2014
- 2014-11-18 CN CN201410658242.XA patent/CN104353258B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2325207C1 (en) * | 2007-01-31 | 2008-05-27 | Валерий Григорьевич Цегельский | Device for vacuum distillation of raw predominantly petroleum raw |
| CN201692678U (en) * | 2010-03-18 | 2011-01-05 | 南京蓝星化工新材料有限公司 | Vacuum system |
| CN204319802U (en) * | 2014-11-18 | 2015-05-13 | 镇海石化工程股份有限公司 | Subtract top pumped vacuum systems |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10207220B2 (en) | 2017-03-15 | 2019-02-19 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for removing sulfur oxides from gas |
| US10016721B1 (en) | 2017-05-25 | 2018-07-10 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desufurization process and apparatus |
| US10092877B1 (en) | 2017-05-25 | 2018-10-09 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10213739B2 (en) | 2017-05-25 | 2019-02-26 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10099170B1 (en) | 2017-06-14 | 2018-10-16 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US10159929B1 (en) | 2017-06-14 | 2018-12-25 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US20190001267A1 (en) | 2017-07-03 | 2019-01-03 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10112145B1 (en) | 2017-09-07 | 2018-10-30 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104353258A (en) | 2015-02-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104353258B (en) | Subtract top pumped vacuum systems and technique | |
| CN112648536A (en) | Fluid infusion type oil-gas mixed transportation device | |
| CN204319802U (en) | Subtract top pumped vacuum systems | |
| EP2136039A2 (en) | Heat pump system, operation procedure therefor and evaporator system | |
| CN206617195U (en) | A kind of large-scale pair of back pressure birotor interchangeable Steam Turbine | |
| CN209922936U (en) | Coal gasification black water flash evaporation treatment system | |
| CN104009588A (en) | Evaporative cooling system for vertical shaft motor | |
| CN206556348U (en) | Synthesize ammoniacal liquor ammonia refrigeration system | |
| CN207108543U (en) | The deaerating type of cycles of boiler feedwater | |
| CN104274991B (en) | A kind of multiple spot pumped vacuum systems and multiple spot vacuum pumping method | |
| CN205269075U (en) | Multi -effect evaporator | |
| CN204388412U (en) | A kind of refrigeration system | |
| CN210384862U (en) | Urea evaporative condenser evacuating device | |
| CN106839650A (en) | Gas in natural gas recovery system and technique | |
| CN107062927B (en) | Multistage condenser reverse cooling noncondensable gas system for sea water desalination and process thereof | |
| CN206919524U (en) | A kind of chilldown system that improves puts into operation the matched tube structure of efficiency | |
| CN206803793U (en) | One kind vacuumizes energy saving system | |
| CN204030863U (en) | A kind of vertical shaft motor evaporative cooling system | |
| CN207195147U (en) | Gas-pressed equipment | |
| CN220070773U (en) | Energy-saving system for caprolactam production | |
| CN214735567U (en) | Vacuum pumping device of pressure reducing tower | |
| CN221071427U (en) | Novel energy-saving vacuum system | |
| CN203810698U (en) | Heat recovering system | |
| CN105737620B (en) | Calcium carbide residual neat recovering system is melted in a kind of small piece of calcium carbide shaping | |
| CN103807999B (en) | Heat energy recovering system |
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 |