CN106031831A - A PVR pressure-difference gas-liquid vapor cycle system - Google Patents
A PVR pressure-difference gas-liquid vapor cycle system Download PDFInfo
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- CN106031831A CN106031831A CN201510109681.XA CN201510109681A CN106031831A CN 106031831 A CN106031831 A CN 106031831A CN 201510109681 A CN201510109681 A CN 201510109681A CN 106031831 A CN106031831 A CN 106031831A
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Abstract
The invention belongs to the technical field of chemical separation, and particularly relates to a PVR pressure-difference gas-liquid vapor cycle system. The system comprises a material feeding pump, a material preheater, a gas compression unit, a heat exchange device and a liquid recovery device. Vapor after being compressed by a compressor is fed into the shell layer of the heat exchanger and subjected to heat exchange. A material to be separated is fed into the tube layer of the heat exchanger through the material feeding pump and the material preheater. The heat exchanger, an evaporator and a pump form a liquid self-cycle pipeline. Overheated liquid in the heat exchanger is vaporized through the evaporator. The heat exchanger is connected to the middle of a rectifying column or a first-stage compressor through a gas pipe. An outlet of the shell layer of the heat exchanger can perform gas liquid separation, wherein the gas enters a next-stage compressor, and the liquid is recovered. A final-stage compressor can be connected to a crystallization device. The system can be used for liquid-liquid separation and separation of liquid soluble salt solutions. A material is subjected to rectification or concentration evaporation in a cycle manner in a low-temperature range, and polymers, carbides, and the like are not liable to be generated, and therefore zero emission of wastes is achieved, the efficiency is high, energy consumption is low and economic value is obvious.
Description
Technical field
The invention belongs to technical field of chemical separation, be specifically related to a kind of PVR pressure reduction gas-liquid steam circulation.
Background technology
Organic rectification separates and uses rectifying column the most always, and in traditional tower, thin film drainage is relatively slow, and gas-liquid connects
Contacting surface specific surface area is less, and efficiency is low, and energy consumption is big, and the process of high-temperature process easily produces secondary pollution, has increased the weight of pollutant
Discharge degree.
The patent of Application No. 201010510541.0: rectifier unit, discloses a kind of rectifier unit, needs heating mechanism to continue
Energy is provided；The patent of Application No. 201220002580.4: rectifying column, discloses a kind of rectifying column, has high concentration residual at the bottom of tower
Liquid is discharged, and causes environmental pollution.
Summary of the invention
For Shortcomings in prior art, the invention provides a kind of PVR pressure reduction gas-liquid steam circulation, solve liquid liquid
Separate, the problem that solid-liquid separation efficiency is low, energy consumption is high, and material can circulate in low temperature range and carry out rectification or concentration and evaporation,
Avoid being caused polymer, carbide contamination environment by high temperature, it is achieved the zero-emission of pollutant.
The present invention realizes above-mentioned technical purpose by techniques below means.
A kind of PVR pressure reduction gas-liquid steam circulation, including material front pump, material preheater, multi-level gas compression heat exchange dress
Put, liquid withdrawal system；
Described material front pump is connected with the tube layer import of material preheater, tube layer outlet and the first order gas pressure of material preheater
The heat exchanger tube layer import of contracting heat-exchanger rig connects；
Described gas compression heat-exchanger rig includes compressor, heat exchanger, vaporizer, pump, gas-liquid separator；
Described compressor inlet is connected with primary steam entrance, and the outlet of compressor is connected with heat exchanger shell import；Described heat exchange
The outlet of device shell is connected with gas-liquid separator, the gas phase pipeline of described gas-liquid separator and the pressure of next stage gas compression heat-exchanger rig
Contracting machine import connects, and the liquid pipe of gas-liquid separator is connected with liquid withdrawal system；Afterbody gas compression heat-exchanger rig
The outlet of heat exchanger shell is connected with material preheater shell import, and the thermal source needed for such material preheater is by afterbody heat exchanger
Aerofluxus provide, just can accomplish total heat recovery；The tube layer of described heat exchanger, vaporizer, pump connects formation liquid self circulation loop；
At least including in described system that two-stage gas compresses heat-exchanger rig, every grade of gas compression heat-exchanger rig at least includes a compression
Machine；
Described vaporizer is additionally provided with overfall, and overfall is provided with the liquid self circulation of overflow pipe and next stage gas compression heat-exchanger rig
Circuit communication, cannot will evaporate completely unnecessary circulating liquid and be flow to by overflow pipe the liquid self circulation loop of next stage.
Described system also includes crystallization apparatus, described crystallization apparatus and vaporizer in afterbody gas compression heat-exchanger rig in system
Overflow pipe connect, can in remaining liq soluble-salt crystallize, reclaim, the mother solution after crystallization can input again through material
Pump enters system；
(1) described system for rectification time, system primary steam is provided by rectifier unit, described rectifier unit include rectifying column and
Reboiler, described reboiler is connected with rectifier bottoms；In described rectifying column, primary steam is provided by reboiler, when filling in system
After full steam, close reboiler steam valve；
The gas phase pipe of described vaporizer and the distributor UNICOM of feed pipe, the liquid line of vaporizer and heat exchanger in the tower of rectifying column
Tube layer, pump connect formed liquid self circulation loop.
Now, the superheated liquid in heat exchanger, gasifies through vaporizer, by the distribution of feed pipe in the gas phase pipe tower with rectifying column
Device UNICOM, unevaporated liquid enters from the liquid outlet of base of evaporator and continues circulating and evaporating liquid self circulation loop.
(2) described system for concentration and evaporation time, described system need the external world provide primary steam, the gas phase pipe of described vaporizer with
The compressor of first order gas compression heat-exchanger rig connects, and the liquid line of vaporizer is connected formation liquid with the tube layer of heat exchanger, pump
Body self circular loop.
Now, the superheated liquid in heat exchanger, gasifies through vaporizer, by gas phase pipe and first order gas compression heat-exchanger rig
Compressor connects, and unevaporated liquid enters from the liquid outlet of base of evaporator and continues circulating and evaporating liquid self circulation loop.
The operation principle of the present invention is:
By material in the external world or rectifier unit offer primary steam gasification tower, material steam is products obtained therefrom steam after rectifying column separates,
Steam is through stage compressor, and from heat exchanger shell, end entrance enters, and through heat exchange, from heat exchanger shell lower end, outlet enters gas
Liquid/gas separator, the gas phase of separator enters subordinate's compressor, and the liquid phase of separator enters liquid withdrawal system.
Material front pump by pending liquid material, injecting material preheater, preheated after, enter heat exchanger, through pervaporation
Device, pump forms liquid self circulation loop, and material forms superheated liquid after heat exchange, and superheated liquid is through vaporizer gasification gas phase and essence
Evaporate feed pipe connection in the tower of tower, or gas phase enters first order compressor.
This device can be used in Liquid liquid Separation, the separation of lipid soluble saline solution.
The invention have the benefit that
(1) vaporization in traditional rectifying column is tower, is outside vaporization now, is directly separated in tower；
(2) at least two-stage heat exchange, efficiency is high；
(3), in tradition separating technology, energy consumption is big, and wastewater flow rate is big；Material of the present invention can circulate in low temperature range carry out rectification or
Concentration and evaporation, is not likely to produce polymer, and carbide etc. causes secondary pollution, it is achieved garbage zero-emission.
(4) apparatus of the present invention are widely used, and can be used for rectification, concentration and evaporation etc., and energy consumption is low, and economic worth is notable.
Accompanying drawing explanation
Fig. 1 is the structure chart of rectifier unit of the present invention.
Fig. 2 is the structure chart of concentration and evaporation of the present invention.
Description of reference numerals is as follows:
1-material front pump, 2-material preheater, 3-compressor, 4-heat exchanger, 5-pump, 6-vaporizer, 7-gas-liquid separator,
8-liquid withdrawal system, 9-rectifying column, 10-reboiler, 11-crystallization apparatus, 12-overflow pipe.
Detailed description of the invention
Below in conjunction with the accompanying drawings and specific embodiment the present invention is further illustrated, but protection scope of the present invention is not limited to
This.
(1) rectification
Rectifier unit includes reboiler 10, rectifying column 9, material front pump 1, material preheater 2, compressor 3, heat exchanger 4,
Pump 5, vaporizer 6, gas-liquid separator 7, gasification installation, liquid withdrawal system, crystallization apparatus.
As raw material then needs crystallization apparatus containing salts substances, then it is not required to crystallization apparatus without salts substances.
Described system primary steam is provided by rectifier unit, and described rectifier unit includes reboiler 10 and rectifying column 9, reboiler 10
It is connected with bottom rectifying column 9；In rectifying column 9, primary steam is provided by reboiler 10, after being full of material steam in system, closes
Close reboiler steam valve；
The import of described compressor 3 is connected with rectifying column 9 top, and compressor 3 outlet is connected with heat exchanger 4 shell import, heat exchange
The outlet of device 4 shell is provided with gas-liquid separator 7, the gas phase pipeline of gas-liquid separator 7 and the compressor inlet of next stage heat-exchanger rig
Connecting, the liquid pipe of separator is connected with liquid withdrawal system 8；The outlet of afterbody heat exchanger shell does not set gas-liquid separator
Directly connect with material preheater 2 shell；The overflow pipe 12 of afterbody vaporizer is connected with crystallization apparatus 11.
Reboiler 10 provides material in primary steam gasification tower, material steam products obtained therefrom steam after rectifying column 9 separates to enter one
Level compressor 3, after compressor 3 compresses temperature raising, gas enters heat exchanger 4 shell and heat exchanger tube layer liquid heat exchange, generating unit
Dividing product condensation water, after going out heat exchanger 4, liquid phase is separated by gas-liquid separator 7, and the gas phase not condensed enters compression system of subordinate
System and vapo(u)rization system continue to reclaim the latent heat in gas phase, and liquid phase enters liquid withdrawal system 8；
Through material front pump 1, treating material is entered material preheater 2, and the thermal source of described material preheater is from afterbody
The aerofluxus of heat exchanger 4, thus can accomplish total heat recovery, after preheating, and liquid entrance first-class heat exchanger, heat exchanger, vaporizer,
Pump connects formation liquid self circulation loop；Superheated liquid in heat exchanger 4 through vaporizer 6 gasify gas phase enter rectifying column 9 tower
Middle feed distributor carries out continuous feed,The liquid self circulation that in vaporizer 6, remaining liq enters next stage through overflow pipe 12 returns
Lu Zhong, the overflow pipe 12 of afterbody is connected with crystallization apparatus 11, until remaining liq after crystallization treatment, reenters thing
Material front pump 1, is again introduced into processing system.
(2) concentration and evaporation
Described concentration and evaporation device includes material front pump 1, material preheater 2, compressor 3, heat exchanger 4, pump 5, evaporation
Device 6, gas-liquid separator 7, crystallization apparatus.
As raw material then needs crystallizer containing salts substances, then it is not required to crystallizer without salts substances.
Steam pipework is connected with first order compressor 3 entrance, and compressor 3 outlet is connected with heat exchanger 4 shell import, heat exchanger
4 shell outlets are provided with gas-liquid separator 7, and gas phase pipeline is connected with the compressor inlet of next stage heat-exchanger rig, fluid pipeline and liquid
Body retracting device 8 connects；The outlet of afterbody heat exchanger shell is provided only with liquid outlet, and liquid outlet is with material preheater 2 even
Logical；Afterbody vaporizer is connected with crystallization apparatus 11.
The extraneous steam that provides, steam entrance stage compressor 3, after compressor 3, gas enters heat exchanger 4 shell, compressed gas
Body is after heat exchange, and generating unit segregation junction liquid, the gas phase not condensed and condensation water are separated under the entrance of gas phase pipe by gas-liquid separator 7
Level compressor 3, liquid enters liquid withdrawal system 8；
Through material front pump 1, treating material is entered material preheater 2, and the thermal source of described material preheater 2 is from last
The aerofluxus of level heat exchanger, thus can accomplish total heat recovery, and after preheating, liquid enters first-class heat exchanger 4, heat exchanger 4, evaporation
Device 6, pump 5 connects formation liquid self circulation loop；Superheated liquid in heat exchanger 4 through vaporizer 6 gasify gas phase enter compression
Machine is compressed temperature raising, and compression high-temperature gas enters heat exchanger shell and tube layer liquid and carries out heat exchange, generating unit segregation junction liquid,
Condensation water and the gas phase not condensed enter gas-liquid separator 7 and separate, and the liquid separated enters liquid withdrawal system 8, and gas enters
Next organizes compression, heat exchange, vapo(u)rization system, and tube layer is entered the liquid phase of heat exchange and obtained superheated liquid, and superheated liquid enters vaporizer 6 gas
Activating QI enters first order compressor compresses temperature raising mutually and enters heat exchanger, such repeated compression, heat exchange, gasify, concentrate, crystallize,
Just under the situation not having outer supplying heat source, the material of required concentration and evaporation is processed,In vaporizer, remaining liq enters through overflow pipe 12
Entering in the liquid self circulation loop of next stage, the overflow pipe 12 of afterbody is connected with crystallization apparatus 11, treats that remaining liq passes through
After crystallization treatment, reenter material front pump 1, be again introduced into processing system.
Described embodiment be the present invention preferred embodiment, but the present invention is not limited to above-mentioned embodiment, without departing substantially from this
In the case of the flesh and blood of invention, any conspicuously improved, replacement or modification that those skilled in the art can make are equal
Belong to protection scope of the present invention.
Claims (6)
1. a PVR pressure reduction gas-liquid steam circulation, it is characterised in that include material front pump (1), material preheater
(2), multi-level gas compression heat-exchanger rig, liquid withdrawal system (8)；
Described material front pump (1) is connected with the tube layer import of material preheater (2), the tube layer outlet of material preheater (2)
It is connected with heat exchanger (4) the tube layer import of first order gas compression heat-exchanger rig；
Described gas compression heat-exchanger rig, including compressor (3), heat exchanger (4), vaporizer (6), pump (5), gas-liquid is divided
From device (7)；
Described compressor (3) import is connected with primary steam entrance, the outlet of compressor (3) and heat exchanger (4) shell import
Connect；The outlet of described heat exchanger (4) shell is connected with gas-liquid separator (7), the gas phase pipeline of described gas-liquid separator (7)
Being connected with compressor (3) import of next stage gas compression heat-exchanger rig, the liquid pipe of gas-liquid separator (7) returns with liquid
Receiving apparatus (8) connects；The outlet of heat exchanger (4) shell and material preheater (2) shell of afterbody gas compression heat-exchanger rig
Layer import connects；The tube layer of described heat exchanger (4), vaporizer (6), pump (5) connects formation liquid self circulation loop.
A kind of PVR pressure reduction gas-liquid steam circulation the most according to claim 1, it is characterised in that in described system extremely
Including that two-stage gas compresses heat-exchanger rig less, every grade of gas compression heat-exchanger rig at least includes a compressor.
A kind of PVR pressure reduction gas-liquid steam circulation the most according to claim 1, it is characterised in that described vaporizer
(6) being additionally provided with overfall, overfall is provided with the liquid self circulation loop of overflow pipe (12) and next stage gas compression heat-exchanger rig
Connection.
A kind of PVR pressure reduction gas-liquid steam circulation the most according to claim 3, it is characterised in that described system is also
Including crystallization apparatus (11), described crystallization apparatus (11) and vaporizer (6) in afterbody gas compression heat-exchanger rig in system
Overflow pipe (12) connect.
A kind of PVR pressure reduction gas-liquid steam circulation the most according to claims 1 to 4, it is characterised in that described system
When rectification, system primary steam is provided by rectifier unit, and described rectifier unit includes rectifying column (9) and reboiler (10),
Described reboiler (10) is connected with rectifying column (9) bottom；Described rectifying column (9) interior primary steam is carried by reboiler (10)
Confession, after being full of steam in system, closes reboiler (10) steam valve；
The gas phase pipe of described vaporizer (6) and the distributor UNICOM of feed pipe, the liquid of vaporizer (6) in the tower of rectifying column (9)
Body pipeline is connected formation liquid self circulation loop with tube layer, the pump (5) of heat exchanger (4).
A kind of PVR pressure reduction gas-liquid steam circulation the most according to claims 1 to 4, it is characterised in that described system
When concentration and evaporation, described system needs the external world to provide primary steam, the gas phase pipe of described vaporizer (6) and first order gas pressure
The compressor (3) of contracting heat-exchanger rig connects, and the liquid line of vaporizer (6) is with the tube layer of heat exchanger (4), pump (5) even
Connect formation liquid self circulation loop.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510109681.XA CN106031831B (en) | 2015-03-12 | 2015-03-12 | A kind of pressure difference gas-liquid steam circulation |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510109681.XA CN106031831B (en) | 2015-03-12 | 2015-03-12 | A kind of pressure difference gas-liquid steam circulation |
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| Publication Number | Publication Date |
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| CN106031831A true CN106031831A (en) | 2016-10-19 |
| CN106031831B CN106031831B (en) | 2018-11-06 |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1325887A1 (en) * | 2001-12-21 | 2003-07-09 | Air Liquide Electronics Systems | Process for producing the solution of a chemical product starting from the liquid phase of a chemical product |
| CN1901980A (en) * | 2003-12-11 | 2007-01-24 | Gea维甘德有限公司 | Evaporation system |
| CN202724715U (en) * | 2012-08-03 | 2013-02-13 | 赵建安 | Improved thermal vapor recompression system |
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2015
- 2015-03-12 CN CN201510109681.XA patent/CN106031831B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1325887A1 (en) * | 2001-12-21 | 2003-07-09 | Air Liquide Electronics Systems | Process for producing the solution of a chemical product starting from the liquid phase of a chemical product |
| CN1901980A (en) * | 2003-12-11 | 2007-01-24 | Gea维甘德有限公司 | Evaporation system |
| CN202724715U (en) * | 2012-08-03 | 2013-02-13 | 赵建安 | Improved thermal vapor recompression system |
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| CN106031831B (en) | 2018-11-06 |
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