CN117146608B - Inclined tower type carbon dioxide condenser and condensation method - Google Patents
Inclined tower type carbon dioxide condenser and condensation method Download PDFInfo
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- CN117146608B CN117146608B CN202311434059.7A CN202311434059A CN117146608B CN 117146608 B CN117146608 B CN 117146608B CN 202311434059 A CN202311434059 A CN 202311434059A CN 117146608 B CN117146608 B CN 117146608B
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- 238000009833 condensation Methods 0.000 title claims abstract description 353
- 230000005494 condensation Effects 0.000 title claims abstract description 353
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 139
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 69
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 69
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 55
- 238000000926 separation method Methods 0.000 claims abstract description 32
- 239000007791 liquid phase Substances 0.000 claims description 151
- 239000003507 refrigerant Substances 0.000 claims description 133
- 239000012071 phase Substances 0.000 claims description 124
- 239000002994 raw material Substances 0.000 claims description 27
- 230000008569 process Effects 0.000 claims description 6
- 230000010354 integration Effects 0.000 abstract description 3
- 230000009467 reduction Effects 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 185
- 238000003466 welding Methods 0.000 description 22
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- HSFWRNGVRCDJHI-UHFFFAOYSA-N Acetylene Chemical compound C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000009965 odorless effect Effects 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000003303 reheating Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910001339 C alloy Inorganic materials 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000012993 chemical processing Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000009920 food preservation Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000008635 plant growth Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000007778 shielded metal arc welding Methods 0.000 description 1
- 235000014214 soft drink Nutrition 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B5/00—Condensers employing a combination of the methods covered by main groups F28B1/00 and F28B3/00; Other condensers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B9/00—Auxiliary systems, arrangements, or devices
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a diagonal tower type carbon dioxide condenser and a condensation method; the condenser comprises a condenser shell which is obliquely arranged, wherein a plurality of baffles are arranged in the condenser shell, the inner part of the condenser shell is divided into a plurality of condensation cavities by the plurality of baffles, and a gas circulation channel is arranged between two adjacent condensation cavities; at least one first heat exchange channel which exchanges heat with the interior of the plurality of condensation cavities is arranged in the condenser shell; the device has the characteristics of small occupied area, high equipment integration level, realization of gas-liquid separation in the condensation cavity, compact equipment structure and reduction of pipeline resistance.
Description
Technical Field
The invention relates to the technical field of carbon dioxide production, in particular to a diagonal tower type carbon dioxide condenser and a condensation method.
Background
Carbon dioxide (carbon dioxide), a carbon oxide, of the formula CO 2 The chemical formula weight is 44.0095, and the gas is colorless, odorless or colorless and odorless gas with slightly sour aqueous solution at normal temperature and normal pressure, has wide application, and uses the gas carbon dioxide in the inert protection, welding gas and plant growth stimulant in the carbonization of soft drink, chemical processing, food preservation, chemical and food processing processes; taking welding gas as an example, the most common welding mode of the hoisting equipment is mixed gas shielded welding and submerged arc automatic welding, wherein the common shielding gas for the mixed gas shielded welding is carbon dioxide. The greatest feature of carbon dioxide gas shielded welding is that it can prevent oxygen in air from contacting with metal melted at high temperature at the welding point, and can protect the metal from oxidation during welding process, so that it has become One of the most important welding methods for ferrous materials. The advantages of carbon dioxide gas shielded welding over general welding are also apparent and may be embodied in the following ways: 1. the welding cost is low, and the cost is only 40-50% of that of arc welding and shielded metal arc welding. 2. The production efficiency is high, and the productivity is 1-4 times of that of the welding rod arc welding. 3. The cracking resistance of the welding seam is high. The weld is low in hydrogen mesh nitrogen content and low in nitrogen content. 4. The post-weld distortion is less. The angle deformation is five thousandths, and the unevenness is only three thousandths; 5. the welding spatter is small. When ultra-low carbon alloy welding wire or flux-cored wire is adopted, or in CO 2 Ar is added in the welding spatter can be reduced. 6. The carbon dioxide gas raw material is very easy to extract and refine, the preparation difficulty in the welding process is reduced to a great extent, the application range is wider, the operation is very simple and convenient, the open arc welding can be carried out, the full-position welding can be carried out, the downward welding can be carried out, the thickness of a workpiece is not limited, and the method is more friendly to operators.
In the purification of carbon dioxide by rectification, secondary or tertiary condensation is generally employed, for example: authorized bulletin number: CN219433611U, patent name: the purifying device for low concentration carbon dioxide has three stages of condensing and separating units in the gas phase outlet in the top of the rectifying tower, the liquid phase outlet of the three stages of condensing and separating units connected to the reflux port of the rectifying liquid in the upper part of the rectifying tower, and the liquid phase outlet in the bottom of the rectifying tower connected via the fourth regulating valve to the high purity carbon dioxide product storing tank; the three-stage condensation separation unit comprises a first-stage condensation separation part, a second-stage condensation separation part and a third-stage condensation separation part, a gas phase outlet at the top of the rectifying tower is connected with the first-stage condensation separation part, a gas phase of the first-stage condensation separation part is connected with the second-stage condensation separation part, a gas phase of the second-stage condensation separation part is connected with the third-stage condensation separation part, and a gas phase of the third-stage condensation separation part is connected with the tail gas treatment device; as can be seen from the above, for the gas phase in the rectifying tower, three-stage condensation separation is required, specifically, a first-stage condensation separator, a first-stage gas-liquid separator, a second-stage condensation separator, a second-stage gas-liquid separator, a main heat exchanger and a third-stage gas-liquid separator are provided, and for reducing energy consumption, vertical arrangement is generally adopted (for example, the setting position of the first-stage condensation separator is higher than that of the second-stage condensation separator, and the setting position of the second-stage condensation separator is higher than that of the main heat exchanger, etc.); the arrangement has the defects of high investment cost, large equipment quantity and large occupied area.
Disclosure of Invention
The invention aims to provide a device and a method for preparing high-purity nitric oxide, which are used for solving the problems in the background technology.
In order to achieve the above purpose, the present invention provides the following technical solutions:
the inclined tower type carbon dioxide condenser comprises a condenser shell which is obliquely arranged, wherein a plurality of baffles are arranged in the condenser shell, the inner part of the condenser shell is divided into a plurality of condensation cavities by the plurality of baffles, and a gas circulation channel is arranged between two adjacent condensation cavities; at least one first heat exchange channel which exchanges heat with the inside of the plurality of condensation cavities is arranged in the condenser shell.
The beneficial effects of the invention are as follows: the primary condensation separator, the secondary condensation separator and the main heat exchanger in the prior art are combined to form the condenser shell which is obliquely arranged, so that the number of equipment is reduced, the investment cost is reduced, and the occupied area of the equipment is reduced; according to the invention, by means of obliquely arranging the condenser shell, liquid-phase carbon dioxide overflow in a plurality of condensing cavities can be prevented, and further, by arranging the gas circulation channels, the gas phase of the upper layer can gradually enter the condensing cavity of the lower layer, so that the purpose of gradual condensation and heat exchange is realized. Furthermore, the invention can realize the purpose of gas-liquid separation while condensing in the condensing cavity by arranging the baffle plate and the gas circulation channel, thereby reducing equipment investment and operating cost.
Preferably, the condensation cavity at the top of the condenser shell is connected with a raw material gas pipeline, the condensation cavity at the bottom of the condenser shell is connected with an exhaust gas pipeline, and the lower parts of the condensation cavities are respectively provided with a liquid phase outlet pipeline; the first heat exchange channel in the condensing cavity at the bottom of the condenser shell is connected with the three-stage refrigerant liquid-phase inlet pipeline, the first heat exchange channel in the condensing cavity at the top of the condenser shell is connected with the three-stage refrigerant gas-phase outlet pipeline, and the first heat exchange channel penetrates through the condensing cavities from bottom to top.
Preferably, the exhaust gas pipeline is connected with an inlet of the gas-liquid separator, a gas phase outlet of the gas-liquid separator is connected with a tail gas heat exchange channel in the condensation cavity at the bottom through a pipeline, and an outlet of the tail gas heat exchange channel in the condensation cavity at the top is connected with a tail gas main pipe; the tail gas heat exchange channel penetrates through the condensation cavities from bottom to top.
Preferably, the condenser shell is internally provided with a first-stage baffle and a second-stage baffle from top to bottom in sequence, and a first-stage condensation cavity is formed between the top of the first-stage baffle and the top of the condenser shell; a third-stage condensation cavity is formed between the bottom of the second-stage baffle and the bottom of the condenser shell; the first-stage baffle and the second-stage baffle form a second-stage condensation cavity in the middle of the condenser shell corresponding to the two baffles.
Preferably, the horizontal included angle between the condenser shell and the ground is 15-85 degrees.
Preferably, the width of the condenser shell is equal to the sum of the length of the baffle and the length of the gas flow channel; the ratio between the length of the first-stage baffle and the width of the condenser shell is 6-8: 10; the ratio between the length of the secondary baffle and the width of the condenser shell is 4-6: 10.
preferably, the lower part of the first-stage condensation cavity is provided with a first-stage liquid-phase carbon dioxide outlet pipeline, the lower part of the second-stage condensation cavity is provided with a second-stage liquid-phase carbon dioxide outlet pipeline, and the lower part of the third-stage condensation cavity is provided with a third-stage liquid-phase carbon dioxide outlet pipeline.
Preferably, the lower part of the secondary condensation cavity is provided with a secondary refrigerant liquid-phase inlet pipeline, and the secondary refrigerant liquid-phase inlet pipeline is connected with a secondary refrigerant gas-phase outlet pipeline at the upper part of the secondary condensation cavity through a second heat exchange channel arranged in the secondary condensation cavity;
preferably, a first-stage refrigerant liquid-phase inlet pipeline is arranged at the lower part of the first-stage condensation cavity, and is connected with a first-stage refrigerant gas-phase outlet pipeline at the upper part of the first-stage condensation cavity through a third heat exchange channel arranged in the first-stage condensation cavity.
The invention also provides a condensation method by using the inclined tower type carbon dioxide condenser, which comprises the steps that raw gas in a raw gas pipeline enters a condensation cavity at the top for condensation, a condensed liquid phase is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, a condensed gas phase enters an adjacent next condensation cavity for further condensation, the further condensed liquid phase is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, the further condensed gas phase gradually enters a condensation cavity at the bottom for condensation, the deep condensation is performed through the condensation cavity at the bottom, the liquid phase after the deep condensation is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, and the gas phase after the deep condensation is discharged outside through an exhaust pipeline.
Preferably, the condensation method comprises the steps of:
step 1: the raw material gas in the raw material gas pipeline enters the first-stage condensation cavity, the first heat exchange channel, the tail gas heat exchange channel and the third heat exchange channel exchange heat with the raw material gas in the first-stage condensation cavity, the liquid phase after heat exchange condensation is discharged outside through the first-stage liquid-phase carbon dioxide outlet pipeline, and the gas phase after heat exchange condensation is accumulated in the first-stage condensation cavity and enters the second-stage condensation cavity through the gas circulation channel;
Step 2: the gas phase entering the secondary condensation cavity is subjected to heat exchange condensation with the first heat exchange channel, the tail gas heat exchange channel and the second heat exchange channel, the liquid phase subjected to heat exchange condensation is discharged outside through a secondary liquid phase carbon dioxide outlet pipeline, the gas phase subjected to heat exchange condensation is accumulated in the secondary condensation cavity and enters the tertiary condensation cavity through the gas circulation channel,
step 3: the gas phase entering the three-stage condensation cavity is subjected to heat exchange condensation with the first heat exchange channel and the tail gas heat exchange channel, the liquid phase after heat exchange condensation is discharged through a three-stage liquid phase carbon dioxide outlet pipeline,
step 4: in the step 3, the gas phase subjected to heat exchange condensation enters a gas-liquid separator through an exhaust pipeline to carry out gas-liquid separation, the gas phase subjected to gas-liquid separation enters a tail gas heat exchange channel to sequentially exchange heat with a three-stage condensation cavity, a second-stage condensation cavity and a first-stage condensation cavity step by step, and the tail gas subjected to heat exchange is discharged outside through a tail gas main pipe;
step 5: the three-stage liquid-phase refrigerant in the three-stage refrigerant liquid-phase inlet pipeline sequentially passes through the three-stage condensation cavity, the second-stage condensation cavity and the first-stage condensation cavity to perform step-by-step heat exchange, and the three-stage gas-phase refrigerant after heat exchange is discharged through the three-stage refrigerant gas-phase outlet pipeline;
Step 6: the second liquid-phase refrigerant in the second refrigerant liquid-phase inlet pipeline enters the second heat exchange channel in the step 2 to exchange heat with the gas phase in the second condensation cavity, and the second gas-phase refrigerant after heat exchange is discharged outside through the second refrigerant gas-phase outlet pipeline;
step 7: and (2) enabling the primary liquid-phase refrigerant in the primary refrigerant liquid-phase inlet pipeline to enter the third heat exchange channel in the step (1) to exchange heat with the gas phase in the primary condensation cavity, and discharging the secondary gas-phase refrigerant after heat exchange through the primary refrigerant gas-phase outlet pipeline.
The invention mainly aims at the design that a multistage condensation structure is needed in the existing carbon dioxide rectification and purification process; the method is characterized in that a multistage condenser is obliquely arranged in the same condenser shell, the materials in each condensation cavity are subjected to gas-liquid separation by utilizing an oblique structure and a baffle plate, so that the characteristic of improving the cold energy utilization rate on the basis of reducing the arrangement of a gas-liquid separator is realized; the device has the characteristics of small occupied area, high equipment integration level, realization of gas-liquid separation in the condensation cavity, compact equipment structure and reduction of pipeline resistance.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Fig. 2 is a schematic structural view of a condenser housing according to the present invention.
In the figure: 1. a condenser housing; 2. a gas flow passage; 3. a first heat exchange channel; 4. a feed gas conduit; 5. an exhaust gas duct; 6. a three-stage refrigerant liquid phase inlet pipeline; 7. a three-stage refrigerant gas phase outlet pipe; 8. a gas-liquid separator; 9. a tail gas heat exchange channel; 10. a tail gas main pipe; 11. a first-stage baffle; 12. a second-stage baffle; 13. a primary condensing cavity; 14. a secondary condensing cavity; 15. a third-stage condensing cavity; 16. a primary liquid carbon dioxide outlet conduit; 17. a secondary liquid carbon dioxide outlet conduit; 18. a three-stage liquid-phase carbon dioxide outlet pipeline; 19. a secondary refrigerant liquid phase inlet conduit; 20. a second heat exchange channel; 21. a secondary refrigerant gas phase outlet conduit; 22. a primary refrigerant liquid phase inlet conduit; 23. a third heat exchange channel; 24. and a primary refrigerant gas phase outlet pipeline.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention.
Referring to fig. 1 and 2, a tower-type carbon dioxide condenser and a condensing method thereof, wherein the condenser comprises a condenser shell 1 which is obliquely arranged, a plurality of baffles are arranged in the condenser shell 1, the plurality of baffles divide the interior of the condenser shell 1 into a plurality of condensing cavities, and a gas circulation channel 2 is arranged between two adjacent condensing cavities; at least one first heat exchange channel 3 which exchanges heat with the inside of a plurality of condensation cavities is arranged in the condenser shell 1. The invention is based on the condenser shell 1 which is obliquely arranged, and is matched with a plurality of baffles and the gas circulation channels 2, so that the high integration of a plurality of condensing cavities can be realized, the occupied area is saved, and the gas-liquid separation can be realized at the same time, so that the investment cost is saved; the plurality of condensation cavities are sequentially arranged from top to bottom, and the gas circulation channel 2 can be a gap between a baffle plate and the inner wall of the condenser shell 1 or can be a pore channel formed on the baffle plate; the raw material gas flows in the condenser shell 1, and can flow from top to bottom or from bottom to top; the flow direction of the refrigerant in the optimized first heat exchange channel 3 is opposite to that of the raw material gas, so that the characteristic of gradually reducing the temperature and carrying out gradual deep cooling heat exchange on the raw material gas is achieved; it should be noted that fig. 2 is a schematic structural view of the condenser housing, and the heat exchange channels are omitted in order to simplify the drawing.
Further, the condensation cavity at the top of the condenser shell 1 is connected with a raw gas pipeline 4, the condensation cavity at the bottom of the condenser shell 1 is connected with an exhaust gas pipeline 5, and the lower parts of the condensation cavities are respectively provided with a liquid phase outlet pipeline; the first heat exchange channel 3 in the condensation cavity at the bottom of the condenser shell 1 is connected with the three-stage refrigerant liquid-phase inlet pipeline 6, the first heat exchange channel 3 in the condensation cavity at the top of the condenser shell 1 is connected with the three-stage refrigerant gas-phase outlet pipeline 7, and the first heat exchange channel 3 penetrates through a plurality of condensation cavities from bottom to top. The invention adopts the mode that the condensation cavity at the top enters the raw material gas preferably, so that the refrigerant enters from the condensation cavity at the bottom, the mode can reduce the flow speed of the raw material gas, and is beneficial to accumulating heat exchange at the lower part, thereby achieving the characteristic of saving the consumption of cold energy, the first heat exchange channel 3 penetrates through a plurality of condensation cavities from bottom to top, and the inclined arrangement of the condenser shell 1 is matched, so that the pipeline resistance and the static pressure of the refrigerant can be reduced on the premise of reducing the liquid level of the refrigerant, and the characteristic of gradually exchanging heat of the raw material gas is realized; the refrigerant in the three-stage refrigerant liquid-phase inlet pipeline 6 can be liquid-phase carbon dioxide, and the temperature of the refrigerant is-50 to-55 ℃.
Further, the exhaust gas pipeline 5 is connected with an inlet of the gas-liquid separator 8, a gas phase outlet of the gas-liquid separator 8 is connected with a tail gas heat exchange channel 9 in a condensation cavity at the bottom through a pipeline, and an outlet of the tail gas heat exchange channel 9 in the condensation cavity at the top is connected with a tail gas main pipe 10; the tail gas heat exchange channel 9 penetrates through the condensation cavities from bottom to top. The arrangement of the invention can realize the reutilization of the cold quantity of the non-condensable gas in deep condensation, thereby saving the subsequent tail gas reheating process, reducing the heat consumption, and realizing the effective recovery of the cold quantity so as to achieve the characteristic of saving the using quantity of the cold in the first heat exchange channel 3; the tail gas temperature of the gas phase of the gas-liquid separator 8 is-50 to-55 ℃; wherein a shutoff valve can be arranged between the gas phase outlet of the gas-liquid separator 8 and the tail gas heat exchange channel 9.
Further, a first-stage baffle 11 and a second-stage baffle 12 are sequentially arranged in the condenser shell 1 from top to bottom, and a first-stage condensation cavity 13 is formed between the top of the first-stage baffle 11 and the top of the condenser shell 1; a third-stage condensation cavity 15 is formed between the bottom of the second-stage baffle 12 and the bottom of the condenser shell 1; the first-stage baffle 11 and the second-stage baffle 12 form a second-stage condensation cavity 14 at the middle part of the condenser shell 1 corresponding to the two baffles. As described above, the inner wall of the condenser shell 1 is matched with the primary baffle 11 and the secondary baffle 12, so that the primary condensation cavity 13, the secondary condensation cavity 14 and the tertiary condensation cavity 15 can be arranged in series, the gas-liquid separator is saved, the use amount of a pipeline is reduced, and the refrigerant cooling capacity is saved; the temperature in the primary condensation cavity 13 is-16 to-18 ℃, the temperature in the secondary condensation cavity 14 is-25 to-35 ℃, and the temperature in the tertiary condensation cavity 15 is-40 to-48 ℃.
Further, the horizontal included angle between the condenser shell 1 and the ground is 15-85 degrees. The condenser shell 1 and the ground are arranged at a horizontal included angle, so that gas-liquid separation can be realized, namely, liquid phase overflow is prevented from flowing into a next condensation cavity after gas-liquid separation, and meanwhile, accumulated condensed gas phase gradually enters the next condensation cavity; secondly, compared with the vertical arrangement, the arrangement can reduce the liquid level of the refrigerant in the heat exchange pipeline, reduce the temperature difference between the bottom temperature and the upper liquid level temperature of the refrigerant, and improve the flow rate of the condensed gas phase so as to achieve the characteristic of saving the using amount of the refrigerant; finally, the arrangement can facilitate the realization of gas-liquid separation; the above included angles may be 15 °, 20 °, 30 °, 40 °, 50 °, 60 °, 70 °, 80 °, and 85 °.
Further, the width of the condenser shell 1 is equal to the sum of the length of the baffle plate and the length of the gas circulation channel 2; the ratio between the length of the primary baffle 11 and the width of the condenser shell 1 is 6-8: 10; the ratio between the length of the secondary baffle 12 and the width of the condenser shell 1 is 4-6: 10. the invention utilizes the baffle to divide the interior of the condenser shell 1 into three temperature zones, and can be specifically set according to working conditions, and mainly according to different liquefaction amounts in different temperature zones in raw material gas, the arrangement can prevent condensed liquid from entering the next condensation cavity to cause cold waste due to supercooling, and simultaneously facilitate the raw material gas to enter the next condensation cavity.
Further, a primary liquid-phase carbon dioxide outlet pipeline 16 is arranged at the lower part of the primary condensation cavity 13, a secondary liquid-phase carbon dioxide outlet pipeline 17 is arranged at the lower part of the secondary condensation cavity 14, and a tertiary liquid-phase carbon dioxide outlet pipeline 18 is arranged at the lower part of the tertiary condensation cavity 15. The liquid phase condensed in each condensation cavity can be conveniently discharged out rapidly through the arrangement.
Further, a second-stage refrigerant liquid-phase inlet pipeline 19 is arranged at the lower part of the second-stage condensation cavity 14, and the second-stage refrigerant liquid-phase inlet pipeline 19 is connected with a second-stage refrigerant gas-phase outlet pipeline 21 at the upper part of the second-stage condensation cavity 14 through a second heat exchange channel 20 arranged in the second-stage condensation cavity 14; the lower part of the primary condensation cavity 13 is provided with a primary refrigerant liquid-phase inlet pipeline 22, and the primary refrigerant liquid-phase inlet pipeline 22 is connected with a primary refrigerant gas-phase outlet pipeline 24 at the upper part of the primary condensation cavity 13 through a third heat exchange channel 23 arranged in the primary condensation cavity 13. The invention can select whether to start the second heat exchange channel 20 and the third heat exchange channel 23 according to the actual working condition, and can control the flow of corresponding refrigerant according to the specific working conditions in the secondary condensation cavity 14 and the primary condensation cavity 13 when in use, so as to achieve the characteristic of adjusting and controlling the temperature of each condensation cavity; the refrigerant in the second-stage refrigerant liquid phase inlet pipeline 19 can be liquid ammonia, the temperature of the liquid ammonia is between-25 ℃ and-30 ℃, the refrigerant in the first-stage refrigerant liquid phase inlet pipeline 22 can be liquid ammonia, and the temperature of the liquid ammonia is between-16 ℃ and-22 ℃.
The invention also provides a condensation method by using the inclined tower type carbon dioxide condenser, which comprises the steps that raw gas in a raw gas pipeline 4 enters a condensation cavity at the top to be condensed, condensed liquid phase is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, condensed gas phase enters an adjacent next condensation cavity to be further condensed, the further condensed liquid phase is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, the further condensed gas phase gradually enters a condensation cavity at the bottom to be condensed, the deep condensed liquid phase is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, and the deep condensed gas phase is discharged outside through a waste gas pipeline 5.
Further, the condensing method specifically includes the following steps:
step 1: the raw material gas in the raw material gas pipeline 4 enters the first-stage condensation cavity 13, the first heat exchange channel 3, the tail gas heat exchange channel 9 and the third heat exchange channel 23 exchange heat with the raw material gas in the first-stage condensation cavity 13, the liquid phase after heat exchange condensation is discharged outside through the first-stage liquid-phase carbon dioxide outlet pipeline 16, and the gas phase after heat exchange condensation is accumulated in the first-stage condensation cavity 13 and enters the second-stage condensation cavity 14 through the gas circulation channel 2;
Step 2: the gas phase entering the secondary condensation cavity 14 is subjected to heat exchange condensation by the first heat exchange channel 3, the tail gas heat exchange channel 9 and the second heat exchange channel 20, the liquid phase subjected to heat exchange condensation is discharged outside through the secondary liquid phase carbon dioxide outlet pipeline 17, the gas phase subjected to heat exchange condensation is accumulated in the secondary condensation cavity 14 and enters the tertiary condensation cavity 15 through the gas circulation channel 2,
step 3: the gas phase entering the three-stage condensation cavity 15 is subjected to heat exchange condensation by the first heat exchange channel 3 and the tail gas heat exchange channel 9, the liquid phase after heat exchange condensation is discharged through the three-stage liquid phase carbon dioxide outlet pipeline 18,
step 4: in the step 3, the gas phase subjected to heat exchange condensation enters a gas-liquid separator 8 through an exhaust pipeline 5 to carry out gas-liquid separation, the gas phase subjected to gas-liquid separation enters a tail gas heat exchange channel 9 to sequentially exchange heat with a three-stage condensation cavity 15, a two-stage condensation cavity 14 and a first-stage condensation cavity 13 step by step, and the tail gas subjected to heat exchange is discharged outside through a tail gas main pipe 10;
step 5: the three-stage liquid-phase refrigerant in the three-stage refrigerant liquid-phase inlet pipeline 6 sequentially passes through the three-stage condensation cavity 15, the two-stage condensation cavity 14 and the first-stage condensation cavity 13 to perform step-by-step heat exchange, and the three-stage gas-phase refrigerant after heat exchange is discharged through the three-stage refrigerant gas-phase outlet pipeline 7;
Step 6: the secondary liquid-phase refrigerant in the secondary refrigerant liquid-phase inlet pipeline 19 enters the second heat exchange channel 20 in the step 2 to exchange heat with the gas phase in the secondary condensation cavity 14, and the secondary gas-phase refrigerant after heat exchange is discharged outside through the secondary refrigerant gas-phase outlet pipeline 21;
step 7: the primary liquid-phase refrigerant in the primary refrigerant liquid-phase inlet pipeline 22 enters the third heat exchange channel 23 in the step 1 to exchange heat with the gas phase in the primary condensation cavity 13, and the secondary gas-phase refrigerant after heat exchange is discharged outside through the primary refrigerant gas-phase outlet pipeline 24.
According to the invention, through the matching of the obliquely arranged condenser shell 1, the baffle plate and the gas circulation channel 2, a plurality of traditional condensation separation parts (condensers) can be integrated into the condenser shell 1, and meanwhile, the characteristics of gas-liquid separation, timely discharging of liquid-phase products and gradual deep cooling of gas phases can be realized; in the invention, the horizontal included angle between the condenser shell 1 and the ground is preferably 15-85 degrees; the arrangement can realize gas-liquid separation, and compared with the vertical arrangement, the liquid level of the refrigerant can be reduced, so that the temperature difference between the temperature of the bottom of the refrigerant and the temperature of the upper liquid level is reduced, and meanwhile, the flow rate of condensed liquid is reduced, so that the aim of improving the heat exchange effect of equipment is fulfilled; furthermore, the invention also uses the waste gas as the refrigerant to effectively recycle the cold energy, thereby saving the reheating procedure in the subsequent process and effectively saving the using amount of the refrigerant in the first heat exchange channel so as to achieve the purposes of energy conservation and consumption reduction.
The invention will now be further described in connection with specific embodiments for a clearer explanation thereof. Specific examples are as follows:
example 1
The inclined tower type carbon dioxide condenser comprises a condenser shell 1 which is obliquely arranged, wherein a plurality of baffles are arranged in the condenser shell 1, the interior of the condenser shell 1 is divided into a plurality of condensation cavities by the baffles, and a gas circulation channel 2 is arranged between two adjacent condensation cavities; at least one first heat exchange channel 3 which exchanges heat with the inside of a plurality of condensation cavities is arranged in the condenser shell 1. The condensation cavity at the top of the condenser shell 1 is connected with a raw gas pipeline 4, the condensation cavity at the bottom of the condenser shell 1 is connected with an exhaust gas pipeline 5, and the lower parts of the condensation cavities are respectively provided with a liquid phase outlet pipeline; the first heat exchange channel 3 in the condensation cavity at the bottom of the condenser shell 1 is connected with the three-stage refrigerant liquid-phase inlet pipeline 6, the first heat exchange channel 3 in the condensation cavity at the top of the condenser shell 1 is connected with the three-stage refrigerant gas-phase outlet pipeline 7, and the first heat exchange channel 3 penetrates through a plurality of condensation cavities from bottom to top. The exhaust pipeline 5 is connected with an inlet of the gas-liquid separator 8, a gas phase outlet of the gas-liquid separator 8 is connected with a tail gas heat exchange channel 9 in a condensation cavity at the bottom through a pipeline, and an outlet of the tail gas heat exchange channel 9 in the condensation cavity at the top is connected with a tail gas main pipe 10; the tail gas heat exchange channel 9 penetrates through the condensation cavities from bottom to top. A first-stage baffle 11 and a second-stage baffle 12 are sequentially arranged in the condenser shell 1 from top to bottom, and a first-stage condensation cavity 13 is formed between the top of the first-stage baffle 11 and the top of the condenser shell 1; a third-stage condensation cavity 15 is formed between the bottom of the second-stage baffle 12 and the bottom of the condenser shell 1; the first-stage baffle 11 and the second-stage baffle 12 form a second-stage condensation cavity 14 at the middle part of the condenser shell 1 corresponding to the two baffles. The horizontal included angle between the condenser shell 1 and the ground is 15-85 degrees. The width of the condenser shell 1 is equal to the sum of the length of the baffle plate and the length of the gas circulation channel 2; the ratio between the length of the primary baffle 11 and the width of the condenser shell 1 is 6:10; the ratio between the length of the secondary baffle 12 and the width of the condenser shell 1 is 4:10. the lower part of the primary condensation cavity 13 is provided with a primary liquid-phase carbon dioxide outlet pipeline 16, the lower part of the secondary condensation cavity 14 is provided with a secondary liquid-phase carbon dioxide outlet pipeline 17, and the lower part of the tertiary condensation cavity 15 is provided with a tertiary liquid-phase carbon dioxide outlet pipeline 18. The lower part of the secondary condensation cavity 14 is provided with a secondary refrigerant liquid-phase inlet pipeline 19, and the secondary refrigerant liquid-phase inlet pipeline 19 is connected with a secondary refrigerant gas-phase outlet pipeline 21 at the upper part of the secondary condensation cavity 14 through a second heat exchange channel 20 arranged in the secondary condensation cavity 14; the lower part of the primary condensation cavity 13 is provided with a primary refrigerant liquid-phase inlet pipeline 22, and the primary refrigerant liquid-phase inlet pipeline 22 is connected with a primary refrigerant gas-phase outlet pipeline 24 at the upper part of the primary condensation cavity 13 through a third heat exchange channel 23 arranged in the primary condensation cavity 13.
A condensation method using a diagonal tower type carbon dioxide condenser comprises the steps that raw material gas in a raw material gas pipeline 4 enters a condensation cavity at the top to be condensed, condensed liquid phase is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, condensed gas phase enters an adjacent next condensation cavity to be further condensed, the further condensed liquid phase is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, the further condensed gas phase gradually enters a condensation cavity at the bottom to be condensed, the deep condensed liquid phase is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, and the deep condensed gas phase is discharged outside through a waste gas pipeline 5.
Example 2
The inclined tower type carbon dioxide condenser comprises a condenser shell 1 which is obliquely arranged, wherein a plurality of baffles are arranged in the condenser shell 1, the interior of the condenser shell 1 is divided into a plurality of condensation cavities by the baffles, and a gas circulation channel 2 is arranged between two adjacent condensation cavities; at least one first heat exchange channel 3 which exchanges heat with the inside of a plurality of condensation cavities is arranged in the condenser shell 1. The condensation cavity at the top of the condenser shell 1 is connected with a raw gas pipeline 4, the condensation cavity at the bottom of the condenser shell 1 is connected with an exhaust gas pipeline 5, and the lower parts of the condensation cavities are respectively provided with a liquid phase outlet pipeline; the first heat exchange channel 3 in the condensation cavity at the bottom of the condenser shell 1 is connected with the three-stage refrigerant liquid-phase inlet pipeline 6, the first heat exchange channel 3 in the condensation cavity at the top of the condenser shell 1 is connected with the three-stage refrigerant gas-phase outlet pipeline 7, and the first heat exchange channel 3 penetrates through a plurality of condensation cavities from bottom to top. The exhaust pipeline 5 is connected with an inlet of the gas-liquid separator 8, a gas phase outlet of the gas-liquid separator 8 is connected with a tail gas heat exchange channel 9 in a condensation cavity at the bottom through a pipeline, and an outlet of the tail gas heat exchange channel 9 in the condensation cavity at the top is connected with a tail gas main pipe 10; the tail gas heat exchange channel 9 penetrates through the condensation cavities from bottom to top. A first-stage baffle 11 and a second-stage baffle 12 are sequentially arranged in the condenser shell 1 from top to bottom, and a first-stage condensation cavity 13 is formed between the top of the first-stage baffle 11 and the top of the condenser shell 1; a third-stage condensation cavity 15 is formed between the bottom of the second-stage baffle 12 and the bottom of the condenser shell 1; the first-stage baffle 11 and the second-stage baffle 12 form a second-stage condensation cavity 14 at the middle part of the condenser shell 1 corresponding to the two baffles. The horizontal included angle between the condenser shell 1 and the ground is 30 degrees. The width of the condenser shell 1 is equal to the sum of the length of the baffle plate and the length of the gas circulation channel 2; the ratio between the length of the primary baffle 11 and the width of the condenser shell 1 is 8:10; the ratio between the length of the secondary baffle 12 and the width of the condenser shell 1 is 6:10. the lower part of the primary condensation cavity 13 is provided with a primary liquid-phase carbon dioxide outlet pipeline 16, the lower part of the secondary condensation cavity 14 is provided with a secondary liquid-phase carbon dioxide outlet pipeline 17, and the lower part of the tertiary condensation cavity 15 is provided with a tertiary liquid-phase carbon dioxide outlet pipeline 18. The lower part of the secondary condensation cavity 14 is provided with a secondary refrigerant liquid-phase inlet pipeline 19, and the secondary refrigerant liquid-phase inlet pipeline 19 is connected with a secondary refrigerant gas-phase outlet pipeline 21 at the upper part of the secondary condensation cavity 14 through a second heat exchange channel 20 arranged in the secondary condensation cavity 14; the lower part of the primary condensation cavity 13 is provided with a primary refrigerant liquid-phase inlet pipeline 22, and the primary refrigerant liquid-phase inlet pipeline 22 is connected with a primary refrigerant gas-phase outlet pipeline 24 at the upper part of the primary condensation cavity 13 through a third heat exchange channel 23 arranged in the primary condensation cavity 13.
A condensation method using a sloped tower carbon dioxide condenser, the condensation method comprising the steps of:
step 1: the raw material gas in the raw material gas pipeline 4 enters the first-stage condensation cavity 13, the first heat exchange channel 3, the tail gas heat exchange channel 9 and the third heat exchange channel 23 exchange heat with the raw material gas in the first-stage condensation cavity 13, the liquid phase after heat exchange condensation is discharged outside through the first-stage liquid-phase carbon dioxide outlet pipeline 16, and the gas phase after heat exchange condensation is accumulated in the first-stage condensation cavity 13 and enters the second-stage condensation cavity 14 through the gas circulation channel 2;
step 2: the gas phase entering the secondary condensation cavity 14 is subjected to heat exchange condensation by the first heat exchange channel 3, the tail gas heat exchange channel 9 and the second heat exchange channel 20, the liquid phase subjected to heat exchange condensation is discharged outside through the secondary liquid phase carbon dioxide outlet pipeline 17, the gas phase subjected to heat exchange condensation is accumulated in the secondary condensation cavity 14 and enters the tertiary condensation cavity 15 through the gas circulation channel 2,
step 3: the gas phase entering the three-stage condensation cavity 15 is subjected to heat exchange condensation by the first heat exchange channel 3 and the tail gas heat exchange channel 9, the liquid phase after heat exchange condensation is discharged through the three-stage liquid phase carbon dioxide outlet pipeline 18,
step 4: in the step 3, the gas phase subjected to heat exchange condensation enters a gas-liquid separator 8 through an exhaust pipeline 5 to carry out gas-liquid separation, the gas phase subjected to gas-liquid separation enters a tail gas heat exchange channel 9 to sequentially exchange heat with a three-stage condensation cavity 15, a two-stage condensation cavity 14 and a first-stage condensation cavity 13 step by step, and the tail gas subjected to heat exchange is discharged outside through a tail gas main pipe 10;
Step 5: the three-stage liquid-phase refrigerant in the three-stage refrigerant liquid-phase inlet pipeline 6 sequentially passes through the three-stage condensation cavity 15, the two-stage condensation cavity 14 and the first-stage condensation cavity 13 to perform step-by-step heat exchange, and the three-stage gas-phase refrigerant after heat exchange is discharged through the three-stage refrigerant gas-phase outlet pipeline 7;
step 6: the secondary liquid-phase refrigerant in the secondary refrigerant liquid-phase inlet pipeline 19 enters the second heat exchange channel 20 in the step 2 to exchange heat with the gas phase in the secondary condensation cavity 14, and the secondary gas-phase refrigerant after heat exchange is discharged outside through the secondary refrigerant gas-phase outlet pipeline 21;
step 7: the primary liquid-phase refrigerant in the primary refrigerant liquid-phase inlet pipeline 22 enters the third heat exchange channel 23 in the step 1 to exchange heat with the gas phase in the primary condensation cavity 13, and the secondary gas-phase refrigerant after heat exchange is discharged outside through the primary refrigerant gas-phase outlet pipeline 24.
Example 3
The inclined tower type carbon dioxide condenser comprises a condenser shell 1 which is obliquely arranged, wherein a plurality of baffles are arranged in the condenser shell 1, the interior of the condenser shell 1 is divided into a plurality of condensation cavities by the baffles, and a gas circulation channel 2 is arranged between two adjacent condensation cavities; at least one first heat exchange channel 3 which exchanges heat with the inside of a plurality of condensation cavities is arranged in the condenser shell 1. The condensation cavity at the top of the condenser shell 1 is connected with a raw gas pipeline 4, the condensation cavity at the bottom of the condenser shell 1 is connected with an exhaust gas pipeline 5, and the lower parts of the condensation cavities are respectively provided with a liquid phase outlet pipeline; the first heat exchange channel 3 in the condensation cavity at the bottom of the condenser shell 1 is connected with the three-stage refrigerant liquid-phase inlet pipeline 6, the first heat exchange channel 3 in the condensation cavity at the top of the condenser shell 1 is connected with the three-stage refrigerant gas-phase outlet pipeline 7, and the first heat exchange channel 3 penetrates through a plurality of condensation cavities from bottom to top. The exhaust pipeline 5 is connected with an inlet of the gas-liquid separator 8, a gas phase outlet of the gas-liquid separator 8 is connected with a tail gas heat exchange channel 9 in a condensation cavity at the bottom through a pipeline, and an outlet of the tail gas heat exchange channel 9 in the condensation cavity at the top is connected with a tail gas main pipe 10; the tail gas heat exchange channel 9 penetrates through the condensation cavities from bottom to top. A first-stage baffle 11 and a second-stage baffle 12 are sequentially arranged in the condenser shell 1 from top to bottom, and a first-stage condensation cavity 13 is formed between the top of the first-stage baffle 11 and the top of the condenser shell 1; a third-stage condensation cavity 15 is formed between the bottom of the second-stage baffle 12 and the bottom of the condenser shell 1; the first-stage baffle 11 and the second-stage baffle 12 form a second-stage condensation cavity 14 at the middle part of the condenser shell 1 corresponding to the two baffles. The horizontal included angle between the condenser shell 1 and the ground is 85 degrees. The width of the condenser shell 1 is equal to the sum of the length of the baffle plate and the length of the gas circulation channel 2; the ratio between the length of the primary baffle 11 and the width of the condenser shell 1 is 7:10; the ratio between the length of the secondary baffle 12 and the width of the condenser shell 1 is 5:10. the lower part of the primary condensation cavity 13 is provided with a primary liquid-phase carbon dioxide outlet pipeline 16, the lower part of the secondary condensation cavity 14 is provided with a secondary liquid-phase carbon dioxide outlet pipeline 17, and the lower part of the tertiary condensation cavity 15 is provided with a tertiary liquid-phase carbon dioxide outlet pipeline 18. The lower part of the secondary condensation cavity 14 is provided with a secondary refrigerant liquid-phase inlet pipeline 19, and the secondary refrigerant liquid-phase inlet pipeline 19 is connected with a secondary refrigerant gas-phase outlet pipeline 21 at the upper part of the secondary condensation cavity 14 through a second heat exchange channel 20 arranged in the secondary condensation cavity 14; the lower part of the primary condensation cavity 13 is provided with a primary refrigerant liquid-phase inlet pipeline 22, and the primary refrigerant liquid-phase inlet pipeline 22 is connected with a primary refrigerant gas-phase outlet pipeline 24 at the upper part of the primary condensation cavity 13 through a third heat exchange channel 23 arranged in the primary condensation cavity 13.
A condensation method using a sloped tower carbon dioxide condenser, the condensation method comprising the steps of:
step 1: the raw material gas in the raw material gas pipeline 4 enters the first-stage condensation cavity 13, the first heat exchange channel 3, the tail gas heat exchange channel 9 and the third heat exchange channel 23 exchange heat with the raw material gas in the first-stage condensation cavity 13, the liquid phase after heat exchange condensation is discharged outside through the first-stage liquid-phase carbon dioxide outlet pipeline 16, and the gas phase after heat exchange condensation is accumulated in the first-stage condensation cavity 13 and enters the second-stage condensation cavity 14 through the gas circulation channel 2;
step 2: the gas phase entering the secondary condensation cavity 14 is subjected to heat exchange condensation by the first heat exchange channel 3, the tail gas heat exchange channel 9 and the second heat exchange channel 20, the liquid phase subjected to heat exchange condensation is discharged outside through the secondary liquid phase carbon dioxide outlet pipeline 17, the gas phase subjected to heat exchange condensation is accumulated in the secondary condensation cavity 14 and enters the tertiary condensation cavity 15 through the gas circulation channel 2,
step 3: the gas phase entering the three-stage condensation cavity 15 is subjected to heat exchange condensation by the first heat exchange channel 3 and the tail gas heat exchange channel 9, the liquid phase after heat exchange condensation is discharged through the three-stage liquid phase carbon dioxide outlet pipeline 18,
step 4: in the step 3, the gas phase subjected to heat exchange condensation enters a gas-liquid separator 8 through an exhaust pipeline 5 to carry out gas-liquid separation, the gas phase subjected to gas-liquid separation enters a tail gas heat exchange channel 9 to sequentially exchange heat with a three-stage condensation cavity 15, a two-stage condensation cavity 14 and a first-stage condensation cavity 13 step by step, and the tail gas subjected to heat exchange is discharged outside through a tail gas main pipe 10;
Step 5: the three-stage liquid-phase refrigerant in the three-stage refrigerant liquid-phase inlet pipeline 6 sequentially passes through the three-stage condensation cavity 15, the two-stage condensation cavity 14 and the first-stage condensation cavity 13 to perform step-by-step heat exchange, and the three-stage gas-phase refrigerant after heat exchange is discharged through the three-stage refrigerant gas-phase outlet pipeline 7;
step 6: the secondary liquid-phase refrigerant in the secondary refrigerant liquid-phase inlet pipeline 19 enters the second heat exchange channel 20 in the step 2 to exchange heat with the gas phase in the secondary condensation cavity 14, and the secondary gas-phase refrigerant after heat exchange is discharged outside through the secondary refrigerant gas-phase outlet pipeline 21;
step 7: the primary liquid-phase refrigerant in the primary refrigerant liquid-phase inlet pipeline 22 enters the third heat exchange channel 23 in the step 1 to exchange heat with the gas phase in the primary condensation cavity 13, and the secondary gas-phase refrigerant after heat exchange is discharged outside through the primary refrigerant gas-phase outlet pipeline 24.
Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (5)
1. A sloped tower carbon dioxide condenser, characterized by: the condenser comprises a condenser shell (1) which is obliquely arranged, wherein a plurality of baffles are arranged in the condenser shell (1), the inner part of the condenser shell (1) is divided into a plurality of condensation cavities by the plurality of baffles, and a gas circulation channel (2) is arranged between two adjacent condensation cavities;
At least one first heat exchange channel (3) which exchanges heat with the interior of a plurality of condensation cavities is arranged in the condenser shell (1);
the width of the condenser shell (1) is equal to the sum of the length of the baffle plate and the length of the gas circulation channel (2);
the condensing cavities at the top of the condenser shell (1) are connected with a raw gas pipeline (4), the condensing cavities at the bottom of the condenser shell (1) are connected with an exhaust gas pipeline (5), and the lower parts of the condensing cavities are respectively provided with a liquid phase outlet pipeline;
a first heat exchange channel (3) in a condensation cavity at the bottom of the condenser shell (1) is connected with a three-stage refrigerant liquid-phase inlet pipeline (6), the first heat exchange channel (3) in the condensation cavity at the top of the condenser shell (1) is connected with a three-stage refrigerant gas-phase outlet pipeline (7), and the first heat exchange channel (3) penetrates through a plurality of condensation cavities from bottom to top;
the exhaust pipeline (5) is connected with the inlet of the gas-liquid separator (8), the gas phase outlet of the gas-liquid separator (8) is connected with the tail gas heat exchange channel (9) in the condensation cavity at the bottom through a pipeline, and the outlet of the tail gas heat exchange channel (9) in the condensation cavity at the top is connected with the tail gas main pipe (10); the tail gas heat exchange channel (9) penetrates through the condensation cavities from bottom to top;
A first-stage baffle (11) and a second-stage baffle (12) are sequentially arranged in the condenser shell (1) from top to bottom, and a first-stage condensation cavity (13) is formed between the top of the first-stage baffle (11) and the top of the condenser shell (1); a third-stage condensation cavity (15) is formed between the bottom of the second-stage baffle (12) and the bottom of the condenser shell (1);
the condenser comprises a first-stage baffle (11) and a second-stage baffle (12), wherein a second-stage condensation cavity (14) is formed in the middle of a condenser shell (1) corresponding to the two baffles;
the lower part of the primary condensation cavity (13) is provided with a primary liquid-phase carbon dioxide outlet pipeline (16), the lower part of the secondary condensation cavity (14) is provided with a secondary liquid-phase carbon dioxide outlet pipeline (17), and the lower part of the tertiary condensation cavity (15) is provided with a tertiary liquid-phase carbon dioxide outlet pipeline (18);
the lower part of the secondary condensation cavity (14) is provided with a secondary refrigerant liquid-phase inlet pipeline (19), and the secondary refrigerant liquid-phase inlet pipeline (19) is connected with a secondary refrigerant gas-phase outlet pipeline (21) at the upper part of the secondary condensation cavity (14) through a second heat exchange channel (20) arranged in the secondary condensation cavity (14);
the lower part of the primary condensation cavity (13) is provided with a primary refrigerant liquid-phase inlet pipeline (22), and the primary refrigerant liquid-phase inlet pipeline (22) is connected with a primary refrigerant gas-phase outlet pipeline (24) at the upper part of the primary condensation cavity (13) through a third heat exchange channel (23) arranged in the primary condensation cavity (13).
2. A sloped tower carbon dioxide condenser in accordance with claim 1, wherein: the horizontal included angle between the condenser shell (1) and the ground is 15-85 degrees.
3. A sloped tower carbon dioxide condenser in accordance with claim 1, wherein: the ratio between the length of the first-stage baffle plate (11) and the width of the condenser shell (1) is 6-8: 10; the ratio between the length of the secondary baffle (12) and the width of the condenser shell (1) is 4-6: 10.
4. a condensation method using the inclined tower type carbon dioxide condenser according to claim 1, characterized in that: the condensation method comprises the steps that raw gas in a raw gas pipeline (4) enters a condensation cavity at the top to be condensed, condensed liquid phase is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, condensed gas phase enters an adjacent next condensation cavity to be further condensed, the further condensed liquid phase is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, the further condensed gas phase gradually enters a condensation cavity at the bottom to be condensed, the deep condensation is performed through the condensation cavity at the bottom, the liquid phase after the deep condensation is discharged outside through a liquid phase outlet pipeline corresponding to the condensation cavity, and the gas phase after the deep condensation is discharged outside through an exhaust gas pipeline (5).
5. The condensation process using a sloped carbon dioxide condenser according to claim 4, wherein: the condensing method comprises the following steps:
step 1: the raw material gas in the raw material gas pipeline (4) enters a first-stage condensation cavity (13), the first heat exchange channel (3), the tail gas heat exchange channel (9) and the third heat exchange channel (23) exchange heat with the raw material gas in the first-stage condensation cavity (13), a liquid phase after heat exchange condensation is discharged outside through a first-stage liquid-phase carbon dioxide outlet pipeline (16), and a gas phase after heat exchange condensation is accumulated in the first-stage condensation cavity (13) and enters a second-stage condensation cavity (14) through a gas circulation channel (2);
step 2: the gas phase entering the secondary condensation cavity (14) is subjected to heat exchange condensation with the first heat exchange channel (3), the tail gas heat exchange channel (9) and the second heat exchange channel (20), the liquid phase after heat exchange condensation is discharged outside through a secondary liquid phase carbon dioxide outlet pipeline (17), the gas phase after heat exchange condensation is accumulated in the secondary condensation cavity (14) and enters the tertiary condensation cavity (15) through the gas circulation channel (2),
step 3: the gas phase entering the three-stage condensation cavity (15) is subjected to heat exchange condensation with the first heat exchange channel (3) and the tail gas heat exchange channel (9), the liquid phase after heat exchange condensation is discharged through a three-stage liquid-phase carbon dioxide outlet pipeline (18),
Step 4: in the step 3, the gas phase subjected to heat exchange condensation enters a gas-liquid separator (8) through an exhaust pipeline (5) to be subjected to gas-liquid separation, and the gas phase subjected to gas-liquid separation enters a tail gas heat exchange channel (9) to be subjected to gradual heat exchange with a three-stage condensation cavity (15), a two-stage condensation cavity (14) and a one-stage condensation cavity (13) in sequence, and the tail gas subjected to heat exchange is discharged through a tail gas main pipe (10);
step 5: the three-stage liquid-phase refrigerant in the three-stage refrigerant liquid-phase inlet pipeline (6) sequentially passes through the three-stage condensation cavity (15), the two-stage condensation cavity (14) and the one-stage condensation cavity (13) to exchange heat step by step, and the three-stage gas-phase refrigerant after heat exchange is discharged outside through the three-stage refrigerant gas-phase outlet pipeline (7);
step 6: the second liquid-phase refrigerant in the second-phase refrigerant liquid-phase inlet pipeline (19) enters the second heat exchange channel (20) in the step 2 to exchange heat with the gas phase in the second-phase condensation cavity (14), and the second-phase refrigerant after heat exchange is discharged outside through the second-phase refrigerant gas-phase outlet pipeline (21);
step 7: the primary liquid-phase refrigerant in the primary refrigerant liquid-phase inlet pipeline (22) enters the third heat exchange channel (23) in the step 1 to exchange heat with the gas phase in the primary condensation cavity (13), and the secondary gas-phase refrigerant after heat exchange is discharged outside through the primary refrigerant gas-phase outlet pipeline (24).
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