CN206126859U - Pure carbon dioxide's of heat pump distillation production superelevation device - Google Patents
Pure carbon dioxide's of heat pump distillation production superelevation device Download PDFInfo
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- CN206126859U CN206126859U CN201621042644.8U CN201621042644U CN206126859U CN 206126859 U CN206126859 U CN 206126859U CN 201621042644 U CN201621042644 U CN 201621042644U CN 206126859 U CN206126859 U CN 206126859U
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- heat exchanger
- raw material
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- gas inlet
- rectifying column
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- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Carbon And Carbon Compounds (AREA)
Abstract
The utility model belongs to a pure carbon dioxide's of heat pump distillation production superelevation device, including raw material liquid storage tank, raw material liquid storage tank passes through a throttling valve set and evaporimeter and a feed gas inlet and links to each other, first rectifying column top gas exports passes through a feed gas inlet of second heat exchanger, a feed gas outlet of second heat exchanger, the tube side of heat pump and third heat exchanger links to each other with first tee bend, first three -way second end links to each other with the import of second reboiler through the 3rd feed gas inlet of second heat exchanger and the 3rd feed gas outlet of second heat exchanger, the export of second reboiler links to each other with a feed gas inlet of second rectifying column, the bottom liquid phase export of second rectifying column is through the product import of fourth heat exchanger and the product export and the product storage tank of fourth heat exchanger, it is simple, easy and simple to handle to have process flow, and operation preparation liquid phase carbon dioxide purity stable and that the comprehensive energy consumption is low is not less than 99.99999% advantage.
Description
Technical field
This utility model belongs to production ultra-high purity carbon dioxide technical field, and in particular to a kind of heat pump distillation produces superelevation
The device of pure carbon dioxide.
Background technology
Carbon dioxide is both a kind of wide material sources, basic chemical raw materials cheap and easy to get, is again the environmental protection of recoverable
Type product, to realizing that low-carbon emission reduction has the important meaning of good economic benefit and environmental conservation.As it is a kind of it is valuable can
Using resource, in having been widely used for the fields such as food industry, machining, oil exploitation, chemical industry.Especially food
Carbon dioxide is used for together for producing soda pop, medicated beer, particularly high-purity carbon dioxide with high-purity helium and high pure nitrogen
The laser gas of laser cutting machine, high-purity carbon dioxide is used for the cell culture such as embryo, the critical extraction of medicine.But sorry
It is to reclaim taking effective measures for carbon dioxide, the carbon dioxide of annual recycling is little, especially high purity liquid carbon dioxide
Production method and device.At present the industrial method for separating carbon dioxide have pressure swing adsorption method, cryogenic distillation process, membrane separation process and
Solution absorption method.These methods respectively have pluses and minuses in specifically used, and low temperature processing is huge due to equipment, energy consumption compared with high score from
Effect is poor, thus relatively costly, is typically rarely employed；Membrane separation process have device simple, life-span length, easy to operate, advanced technology,
Efficiency high, energy consumption are low, economical rationality the advantages of but the shortcoming of membrane separation process is to hardly result in highly purified carbon dioxide, in order to
Obtaining highly purified carbon dioxide must combine with solution absorption method.The former does smart separation for crude separation the latter, but
Its technique is extremely complex；Pressure swing adsorption method energy consumption is low, strong adaptability but to there is also shortcoming be exactly to hardly result in highly purified two
Carbonoxide, and technological process is complicated.
Utility model content
The purpose of this utility model is to overcome of the prior art not enough and provide a kind of using heat pump distillation, multiple-effect essence
Evaporate, technological process is simple, easy to operate, the stable and low preparation liquid phase carbon dioxide purity of comprehensive energy consumption is not less than
A kind of 99.99999% heat pump distillation produces the device of ultra-high purity carbon dioxide.
What the purpose of this utility model was realized in：Including raw material liquid storage tank, raw material liquid storage tank passes through first throttle valve
Group and vaporizer are connected with the first raw material gas inlet of first rectifying column, and the gaseous phase outlet at the top of first rectifying column passes sequentially through the
First raw material gas inlet of two heat exchangers, the tube side of the outlet of the first unstripped gas, heat pump and the 3rd heat exchanger of the second heat exchanger with
First threeway is connected, and the second end of the first threeway passes through the 3rd raw material gas inlet of the second heat exchanger and the 3rd of the second heat exchanger the
Unstripped gas outlet is connected with the second reboiler import of Second distillation column bottom, and the outlet of the second reboiler is by the 4th throttling valve group
It is connected with the first raw material gas inlet of Second distillation column, the bottom liquid phases outlet of Second distillation column passes through the product of the 4th heat exchanger
Import and the products export and product storage tank of the 4th heat exchanger；The liquid-phase outlet of first rectifying column bottom is by the 3rd throttling valve group
Be connected with exhausting pipeline with the inlet exhaust gas of the 4th heat exchanger and the offgas outlet of the 4th heat exchanger, the 3rd end of the first threeway according to
Secondary the second raw material gas inlet for passing through the second heat exchanger, the second unstripped gas outlet of the second heat exchanger, first rectifying column inner bottom part
The first reboiler and second throttle group be connected with the second raw material gas inlet of first rectifying column；Gas at the top of Second distillation column
Mutually outlet is connected by being located at the First Heat Exchanger of vaporizer inner bottom part with gas-liquid separator, the liquid-phase outlet of gas-liquid separator and
Second material inlet of Second distillation column is connected, and the gaseous phase outlet of gas-liquid separator is connected by pipeline with exhausting pipeline；3rd
The shell side of heat exchanger is provided with filling pipe end and water return outlet, and the filling pipe end is connected with circulation water supply pipeline, water return outlet with loop back
Waterpipe is connected.
Preferably, the first raw material gas inlet of the first rectifying column is located at the middle part of first rectifying column；First rectifying column
The second raw material gas inlet be located at the top of first rectifying column.
Preferably, the first raw material gas inlet of the Second distillation column and the second material inlet of Second distillation column set respectively
On the top of Second distillation column.
This utility model from as cold-producing medium, heat and cold is provided by heat pump techniques with feed carbon dioxide for system
Amount, is heated up by the pressurization of rectifying column tower top steam so as to which, used as the thermal source of tower bottom reboiler, the condensation for reclaiming overhead vapours is dived
Heat；It is cold by tower bottom reboiler that this utility model overcomes traditional view to be changed to cold-producing medium by the liquefied ammonia refrigeration in traditional handicraft
The liquid carbon dioxide refrigeration got off is coagulated, the degree of reversibility of distillation process is such a construction increases, energy is drastically increased
Utilization ratio, also improves the safety coefficient in its production while cooling flow is significantly simplified, and compare traditional handicraft
There is revolutionary progress；It is simple, easy to operate with technological process, the stable and low preparation liquid phase dioxy of comprehensive energy consumption
Change the advantage that carbon purity is not less than 99.99999%.
Description of the drawings
Fig. 1 is structural representation of the present utility model.
Specific embodiment
In order to be more clearly understood to technical characteristic of the present utility model, purpose and effect, now control is illustrated
Specific embodiment of the present utility model, in the various figures identical label represent identical part.To make simplified form, in each figure
The part related to utility model is only schematically show, they do not represent it as the practical structures of product.
As shown in figure 1, this utility model includes raw material liquid storage tank 1, raw material liquid storage tank 1 is by first throttle valve group 2 and steams
Send out device 3 to be connected with the first raw material gas inlet 22 of first rectifying column 4, the gaseous phase outlet 26 at the top of first rectifying column 4 is passed sequentially through
First raw material gas inlet 29 of the second heat exchanger 5, the first unstripped gas outlet 32, heat exchanger of heat pump 6 and the 3rd of the second heat exchanger 5
7 tube side is connected with the first threeway 19, and the second end of the first threeway 19 passes through the He of the 3rd raw material gas inlet 27 of the second heat exchanger 5
The 3rd unstripped gas outlet 31 of the second heat exchanger 5 is connected with the import of the second reboiler 12 of the bottom of Second distillation column 13, and second again
The outlet of boiling device 12 is connected by the 4th throttling valve group 14 with the first raw material gas inlet 40 of Second distillation column 13, Second distillation column 13
The products exports 25 and product that pass through the heat exchangers 11 of product import 18 and the 4th of the 4th heat exchanger 11 of bottom liquid phases outlet 41
Storage tank 17；The inlet exhaust gas that the liquid-phase outlet 24 of the bottom of first rectifying column 4 passes through the 3rd throttling heat exchanger 11 of valve group 10 and the 4th
23 and the 4th the offgas outlet 33 of heat exchanger 11 be connected with exhausting pipeline 20, the 3rd end of the first threeway 19 passes sequentially through second and changes
Second raw material gas inlet 28 of hot device 5, the of the second unstripped gas outlet 30, inner bottom part of first rectifying column 4 of the second heat exchanger 5
One reboiler 8 and second throttle group 9 are connected with the second raw material gas inlet 21 of first rectifying column 4；The top of Second distillation column 13
Gaseous phase outlet 39 be connected with gas-liquid separator 15 by being located at the First Heat Exchanger 16 of the inner bottom part of vaporizer 3, gas-liquid separator
15 liquid-phase outlet 34 is connected with the second material inlet 37 of Second distillation column 13, and the gaseous phase outlet 35 of gas-liquid separator 15 passes through
Pipeline is connected with exhausting pipeline 20；The shell side of the 3rd heat exchanger 7 is provided with filling pipe end and water return outlet, on the filling pipe end and circulation
Waterpipe 38 is connected, and water return outlet is connected with circulating backwater pipeline 36.
Preferably, the first raw material gas inlet 22 of the first rectifying column 4 is located at the middle part of first rectifying column 4；First is smart
The second raw material gas inlet 21 for evaporating tower 4 is located at the top of first rectifying column 4.
Preferably, first raw material gas inlet 40 and the second material inlet of Second distillation column 13 of the Second distillation column 13
37 tops for being respectively provided at Second distillation column 13.
A kind of production method of the device of heat pump distillation production ultra-high purity carbon dioxide, comprises the steps：
Step one：Industrial grade carbon-dioxide in raw material liquid storage tank 1 is smart by first throttle valve group 2, vaporizer 3 and first
The first raw material gas inlet 22 for evaporating tower 4 is entered in first rectifying column 4；The main constituents of described industrial grade carbon-dioxide
For：Carbon dioxide, hydrogen, nitrogen, methane, oxygen, carbon monoxide, sulfur dioxide, benzene, methanol, ethanol, water, carbonyl sulfide and
Ethane；Technical grade carbon dioxide temperature is：-22℃；Gas phase fraction is 0, and the molar fraction of carbon dioxide is 99.8%；Jing first
The temperature of the postindustrial grade carbon-dioxide of choke valve 2 is：-28℃；The technical grade dioxy of first raw material gas inlet 22 of first rectifying column 4
Change carbon temperature be：- 28 DEG C, gas phase fraction is 1；
Step 2：The industrial grade carbon-dioxide entered in first rectifying column 4 described in step one is set to carry out rectification and purification, essence
Evaporate the gas phase after purification by the top gas phase of first rectifying column 4 export the 26, second heat exchanger 5 the first raw material gas inlet 29,
The first unstripped gas outlet 32, tube side of the heat exchanger 7 of heat pump 6 and the 3rd of the second heat exchanger 5 is entered in the first threeway 19；It is described
The 3rd heat exchanger 7 shell side in recirculated water and the 3rd heat exchanger 7 tube side in unstripped gas carry out heat exchange cooling, circulate
The recirculated water of 25 DEG C in water supply pipeline 38 is entered in the shell side of the 3rd heat exchanger 7 by the shell side filling pipe end of the 3rd heat exchanger 7, heat exchange
Circulating water temperature afterwards is：33 DEG C, the recirculated water after heat exchange is entered into by the shell side water return outlet of the 3rd heat exchanger 7 and loops back water pipe
In road 36；The top gas phase of the first rectifying column 4 exports 26 unstripped gas temperature：- 20 DEG C, the molar fraction of carbon dioxide
For 99.81%；
Step 3：A part of unstripped gas in the first threeway of entrance 19 described in step 2 in unstripped gas is changed by second
3rd raw material gas inlet 27 of hot device 5, the 3rd unstripped gas of the second heat exchanger 5 export the 31, second reboiler 12, the 4th choke valve
First raw material gas inlet 40 of group 14 and Second distillation column 13 is entered in Second distillation column 13；Described a part of unstripped gas enters
Entering the temperature after the second reboiler 12 is：- 24 DEG C, its state is changed into liquid phase from gas phase, and liquid phase feed is by the 4th throttling valve group
Enter in Second distillation column 13 after 14 throttlings；
Step 4：The liquid phase feed in the entrance Second distillation column 13 described in step 3 is set to carry out rectification and purification, rectification
Liquid phase after purification is changed by the product import 18 and the 4th that the bottom liquid phases of Second distillation column 13 export the 41, the 4th heat exchanger 11
The products export 25 of hot device 11 is entered in product storage tank 17；The liquid phase of the bottom liquid phases outlet 41 of described Second distillation column 13
The temperature of product is：- 19 DEG C, the temperature of the liquid-phase product of the products export 25 of the 4th heat exchanger 11 is：- 24 DEG C, gas phase fraction
0；Product purity reaches 99.99999%；
Step 5：Industrial grade carbon-dioxide described in step 2 passes through the rectification and purification of first rectifying column 4, after rectification and purification
Liquid phase export the 24, the 3rd choke valve 10, the and of inlet exhaust gas 23 of the 4th heat exchanger 11 by the bottom liquid phases of first rectifying column 4
The offgas outlet 33 of the 4th heat exchanger 11 is entered in exhausting pipeline 20 and is vented；The bottom liquid phases outlet 24 of first rectifying column 4 is given up
Liquid temp is：-28℃；The waste liquid temperature of the offgas outlet 33 of the 4th heat exchanger 11 is：-20℃；
Step 6：Another part unstripped gas in the first threeway of entrance 19 described in step 2 in unstripped gas passes through second
Second raw material gas inlet 28 of heat exchanger 5,30, first reboiler of the second unstripped gas outlet 8, second of the second heat exchanger 5 throttle
Second raw material gas inlet 21 of valve group 9 and first rectifying column 4 is entered in first rectifying column 4；The second of the second described heat exchanger 5
Unstripped gas exports 30 unstripped gas temperature：-15℃；
Step 7：Liquid phase feed described in step 4 carries out rectification and purification, rectification and purification in Second distillation column 13
Gas phase afterwards passes through the top gas phase outlet 39 of Second distillation column 13 and First Heat Exchanger 16 to be carried out in gas-liquid separator 15
Gas-liquid separation, the tail gas after gas-liquid separation enters emptying in exhausting pipeline 20 by the gaseous phase outlet 35 of gas-liquid separator 15；Gas
Liquid phase after liquid is separated is entered by the liquid-phase outlet 34 of gas-liquid separator 15 and the second material inlet 37 of Second distillation column 13
In Second distillation column 13；The temperature of tail gas is in the top gas phase outlet 35 of the gas-liquid separator 15：- 24 DEG C, carbon dioxide
Molar fraction 87%；The bottom liquid phases of gas-liquid separator 15 export 34 liquidus temperature：-24℃.
This utility model is a kind of device and production method of heat pump distillation production ultra-high purity carbon dioxide, wherein ultra-pure
Carbon dioxide illustrates that product purity reaches 99.99999% at home without related definition in international higher standard
Carbon dioxide is referred to as ultra-high purity carbon dioxide, and the ultra-high purity carbon dioxide title in this utility model derives from this, and its is concrete
With reference to document be：《Chinese industrial gas is complete works of》3rd, Chinese gas industry association compiles, and publishing house of Dalian University of Technology goes out
Version, the 2575th page table II.2.10-30 foreign countries gas companies high-purity carbon dioxide quality and technical index.This utility model raw material
The cold of liquid itself improves system energy as the fixed gas and heat pump distillation technology that cold-producing medium is used for condensation purification column overhead
The utilization ratio of amount, overcomes the higher shortcoming of the energy consumption of low temperature processing, with two-tower rectification technology overcome membrane separation process and
The technological process complexity of solution absorption method and the low shortcoming of purity.And this utility model technological process is than pressure swing adsorption method flow process
Simply, high degree of automation, the utilization ratio of energy are high.General high-purity carbon dioxide product requirement：Carbon dioxide purity >=
99.99%, total sulfur≤0.2 × 10-6, methanol≤0.1 × 10-6, and the carbon dioxide purity of this utility model production is up to
99.99999%, quality fully meets the requirement of state food grade carbon-dioxide standard and national high-purity carbon dioxide standard,
Domestic high-purity carbon dioxide production is filled up blank, with good economic benefit and social benefit；In addition, this utility model rectification
System adopts heat pump distillation technology, and the heat for dexterously discharging tower top is used for reboiler, it is not necessary to external heat source, reduces
Energy consumption, overcomes traditional view that cold-producing medium is changed to into the liquid condensed out by tower bottom reboiler by the liquefied ammonia refrigeration in traditional handicraft
State carbon dioxide refrigeration, such a construction increases the degree of reversibility of distillation process, drastically increase the utilization ratio of energy,
The safety coefficient in its production is also improved while significantly simplifying cooling flow, the traditional handicraft that compares has revolutionary
It is progressive；The operating unit additionally do not added using two-tower rectification in liquefaction process in process of the present utility model, with
Absorption distillation method compares that its investment of production equipment low cost, energy consumption be low, product profit space is big.Made with the cold of material liquid itself
The fixed gas for being used for condensation purification column overhead for refrigeration dosage drastically increases the utilization rate of energy, reduces system itself
Energy loss.This utility model has the characteristics of technological process is simple, easy to operate, stable, energy utilization efficiency is high,
Recovery rate of CO 2 has reached surprising 93.33% in material liquid.
Those listed above is a series of to describe the tool for being only for feasibility embodiment of the present utility model in detail
Body illustrates that they are simultaneously not used to limit protection domain of the present utility model, all to be made without departing from this utility model skill spirit
Equivalent implementations or change should be included within protection domain of the present utility model.
Claims (3)
1. a kind of heat pump distillation produces the device of ultra-high purity carbon dioxide, it is characterised in that：Including raw material liquid storage tank (1), raw material
The first raw material gas inlet (22) phase that liquid storage tank (1) passes through first throttle valve group (2) and vaporizer (3) and first rectifying column (4)
Even, the gaseous phase outlet (26) at the top of first rectifying column (4) pass sequentially through the second heat exchanger (5) the first raw material gas inlet (29),
Tube side and first threeway (19) of first unstripped gas outlet (32), heat pump (6) and the 3rd heat exchanger (7) of the second heat exchanger (5)
It is connected, the second end of the first threeway (19) passes through the 3rd raw material gas inlet (27) and the second heat exchanger (5) of the second heat exchanger (5)
The 3rd unstripped gas outlet (31) be connected with the second reboiler (12) import of Second distillation column (13) bottom, the second reboiler
(12) outlet is connected by the 4th throttling valve group (14) with first raw material gas inlet (40) of Second distillation column (13), the second rectification
Bottom liquid phases outlet (41) of tower (13) are by the product import (18) of the 4th heat exchanger (11) and the product of the 4th heat exchanger (11)
Product export (25) and product storage tank (17)；The liquid-phase outlet (24) of first rectifying column (4) bottom is by the 3rd throttling valve group (10)
With the inlet exhaust gas (23) of the 4th heat exchanger (11) and the offgas outlet (33) of the 4th heat exchanger (11) and exhausting pipeline (20) phase
Even, the 3rd end of the first threeway (19) passes sequentially through the second raw material gas inlet (28), second heat exchanger of the second heat exchanger (5)
(5) the second unstripped gas outlet (30), first reboiler (8) of first rectifying column (4) inner bottom part and second throttle group (9) and
Second raw material gas inlet (21) of first rectifying column (4) is connected；Gaseous phase outlet (39) at the top of Second distillation column (13) is by setting
It is connected with gas-liquid separator (15) in the First Heat Exchanger (16) of vaporizer (3) inner bottom part, the liquid phase of gas-liquid separator (15) goes out
Mouth (34) is connected with second material inlet (37) of Second distillation column (13), and the gaseous phase outlet (35) of gas-liquid separator (15) passes through
Pipeline is connected with exhausting pipeline (20)；The shell side of the 3rd heat exchanger (7) is provided with filling pipe end and water return outlet, the filling pipe end with follow
Ring water supply pipeline (38) is connected, and water return outlet is connected with circulating backwater pipeline (36).
2. a kind of heat pump distillation according to claim 1 produces the device of ultra-high purity carbon dioxide, it is characterised in that：It is described
First raw material gas inlet (22) of first rectifying column (4) is located at the middle part of first rectifying column (4)；The second of first rectifying column (4)
Raw material gas inlet (21) is located at the top of first rectifying column (4).
3. a kind of heat pump distillation according to claim 1 produces the device of ultra-high purity carbon dioxide, it is characterised in that：It is described
First raw material gas inlet (40) of Second distillation column (13) and second material inlet (37) of Second distillation column (13) are respectively provided at
The top of Second distillation column (13).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621042644.8U CN206126859U (en) | 2016-08-29 | 2016-08-29 | Pure carbon dioxide's of heat pump distillation production superelevation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621042644.8U CN206126859U (en) | 2016-08-29 | 2016-08-29 | Pure carbon dioxide's of heat pump distillation production superelevation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206126859U true CN206126859U (en) | 2017-04-26 |
Family
ID=58568067
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201621042644.8U Withdrawn - After Issue CN206126859U (en) | 2016-08-29 | 2016-08-29 | Pure carbon dioxide's of heat pump distillation production superelevation device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206126859U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106477577A (en) * | 2016-08-29 | 2017-03-08 | 新疆深冷气体有限公司 | A kind of heat pump distillation produces device and the production method of ultra-high purity carbon dioxide |
| CN107174832A (en) * | 2017-06-15 | 2017-09-19 | 重庆川茂化工科技有限公司 | Gas purification high-purity distillation technology and equipment |
-
2016
- 2016-08-29 CN CN201621042644.8U patent/CN206126859U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106477577A (en) * | 2016-08-29 | 2017-03-08 | 新疆深冷气体有限公司 | A kind of heat pump distillation produces device and the production method of ultra-high purity carbon dioxide |
| CN106477577B (en) * | 2016-08-29 | 2019-01-18 | 新疆深冷气体有限公司 | A kind of device and production method of heat pump distillation production ultra-high purity carbon dioxide |
| CN107174832A (en) * | 2017-06-15 | 2017-09-19 | 重庆川茂化工科技有限公司 | Gas purification high-purity distillation technology and equipment |
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| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20170426 Effective date of abandoning: 20190118 |
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| AV01 | Patent right actively abandoned |