CN110801639B - Method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas - Google Patents
Method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas Download PDFInfo
- Publication number
- CN110801639B CN110801639B CN201911094021.3A CN201911094021A CN110801639B CN 110801639 B CN110801639 B CN 110801639B CN 201911094021 A CN201911094021 A CN 201911094021A CN 110801639 B CN110801639 B CN 110801639B
- Authority
- CN
- China
- Prior art keywords
- pipeline
- gas
- refrigeration
- ammonia
- product storage
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000005057 refrigeration Methods 0.000 title claims abstract description 124
- 238000000034 method Methods 0.000 title claims abstract description 46
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 44
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 18
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 278
- 238000003860 storage Methods 0.000 claims abstract description 130
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 103
- 239000007788 liquid Substances 0.000 claims abstract description 47
- 238000001704 evaporation Methods 0.000 claims abstract description 21
- 230000008020 evaporation Effects 0.000 claims abstract description 21
- 239000002994 raw material Substances 0.000 claims abstract description 20
- 238000000746 purification Methods 0.000 claims abstract description 8
- 238000009833 condensation Methods 0.000 claims abstract description 7
- 230000005494 condensation Effects 0.000 claims abstract description 7
- 238000007738 vacuum evaporation Methods 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 149
- 239000000463 material Substances 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 11
- 239000003507 refrigerant Substances 0.000 claims description 10
- 230000006837 decompression Effects 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 239000002699 waste material Substances 0.000 claims description 7
- 238000004781 supercooling Methods 0.000 claims description 4
- 230000018044 dehydration Effects 0.000 claims description 2
- 238000006297 dehydration reaction Methods 0.000 claims description 2
- 238000001035 drying Methods 0.000 claims description 2
- 238000003466 welding Methods 0.000 claims description 2
- 239000002912 waste gas Substances 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 238000011084 recovery Methods 0.000 description 14
- 238000005265 energy consumption Methods 0.000 description 13
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 6
- 235000011089 carbon dioxide Nutrition 0.000 description 4
- 238000000926 separation method Methods 0.000 description 3
- 230000035939 shock Effects 0.000 description 3
- 239000003245 coal Substances 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- XSHGVIPHMOTDCS-UHFFFAOYSA-N 1-(5-fluoropentyl)-n-(2-phenylpropan-2-yl)indazole-3-carboxamide Chemical compound N=1N(CCCCCF)C2=CC=CC=C2C=1C(=O)NC(C)(C)C1=CC=CC=C1 XSHGVIPHMOTDCS-UHFFFAOYSA-N 0.000 description 1
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 1
- 241000282414 Homo sapiens Species 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000013016 damping Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0036—Multiple-effect condensation; Fractional condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- 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
-
- 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
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
-
- 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a method for recovering carbon dioxide by multistage liquefaction and graded refrigeration of industrial tail gas, which comprises the following steps: the raw material gas firstly enters a first residual cold recoverer, is pre-cooled to 22 ℃ by exchanging heat with the non-condensable gas, then enters a second residual cold recoverer, and is pre-cooled to 16 ℃ by exchanging heat with the non-condensable gas. Then to the primary condenser, cooled to-18 ℃ by ammonia evaporative refrigeration, then to the secondary condenser, cooled to-25 ℃ again by ammonia evaporative refrigeration. Then the gas is sent to a rectifying tower for rectification and purification, a tail condenser arranged at the top of the rectifying tower cools tail condensation gas to-45 ℃ through ammonia vacuum evaporation, so that qualified industrial grade or food grade liquid CO is extracted from the tower kettle of the rectifying tower2And (5) producing the product. Then sent to a subcooler through a product pipeline, subcooled to-25 ℃ through ammonia evaporation refrigeration, and then sent to a product storage tank through a product pipeline. The invention has clear process flow, low working pressure and low equipment manufacturing difficulty, improves the refrigeration coefficient of a refrigeration system, and simultaneously improves CO2The system yield can achieve the purposes of energy saving and consumption reduction.
Description
Technical Field
The invention belongs to the technical field of carbon dioxide recovery, and particularly relates to a method for recovering carbon dioxide by multistage liquefaction and stage refrigeration of industrial tail gas.
Background
At present, coal and oil are still main consumption energy of human beings, and in a primary energy consumption structure, coal accounts for 68.5%, oil accounts for 17.7%, natural gas only accounts for 4.7%, and the world average level is far lower than 24%. In the later stage of the regeneration of the decarbonizing solution of the low-temperature methanol decarbonizing device and the early stage of the regeneration of the adsorbent of the PSA decarbonizing device, a tail gas with low and medium carbon dioxide concentration (75-85%) is generated.
In view of the above problems, Chinese patent No. 2018.03.10 discloses a utility model named as a two-stage flash evaporation gas recycling system (application No. CN201820326875.4) of a low-temperature methanol washing flash evaporation tower, in which liquid CO is introduced into the system2The recovery system comprises a fine desulfurization tower and a purification deviceColumn, CO2Gas compressor, precooler, ammonia condenser, separation tower and product CO2A storage tank; the flash gas passes through a water cooling device and then enters a fine desulfurization tower, the desulfurized flash gas enters a purification tower, high-boiling-point substances such as methanol, water and the like in the flash gas are adsorbed in the purification tower, and the flash gas passing through the purification tower enters CO2Pressurizing to 3.4-3.6MPa in two stages of a gas compressor, then feeding into a precooler, cooling and liquefying in an ammonia removal condenser, and finally feeding into a separation tower, and feeding liquid CO2Separating the CO from the non-condensable gas, and separating the liquid CO from the bottom of the separation tower2Entering into product CO2Storage tank capable of producing industrial grade liquid CO2The market price is slightly higher than the production cost, and simultaneously CO is avoided2Environmental impact of gas emissions, but the liquid CO mentioned above2The recovery system has low recovery rate of the recovered carbon dioxide and high energy consumption of the device.
Disclosure of Invention
The invention aims to solve the defects in the prior art, provides the method for recovering the carbon dioxide by multistage liquefaction and graded refrigeration of the industrial tail gas, has clear layers, low working pressure and low equipment manufacturing difficulty, improves the refrigeration coefficient of a refrigeration system, and simultaneously improves the CO2The system yield achieves the purposes of energy conservation and consumption reduction; through the double residual cold recovery operation, the problem that dry ice generated after the high-pressure and low-temperature noncondensable gas is decompressed blocks pipelines and equipment is avoided; the adoption of the multistage liquefaction process corresponding to the staged refrigeration greatly improves the heat cycle efficiency and the refrigeration coefficient of the refrigeration system and reduces the energy consumption of the system.
In order to solve the technical problems, the invention adopts the following technical scheme:
a method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas is characterized by comprising the following steps: the dried and dehydrated feed gas firstly enters a first residual cooling recoverer (101) through a feed gas pipeline (1), is pre-cooled to 22 ℃ through heat exchange with the non-condensable gas, then enters a second residual cooling recoverer (102) through a feed gas pipeline (2), and is pre-cooled to 16 ℃ through heat exchange with the non-condensable gas. Then the gas is subjected to stage refrigeration by a refrigeration system, is sent to a first-stage condenser (104) through a raw material gas pipeline (3), is cooled to-18 ℃ through ammonia evaporation refrigeration, and is then cooledThe raw material gas enters a secondary condenser (105) through a raw material gas-liquid mixing pipeline (4), and is cooled to-25 ℃ through ammonia evaporation refrigeration again. Then the raw material gas enters a rectifying tower (106) through a raw material gas-liquid mixing pipeline (5), rectification and purification are carried out, a tail condenser arranged at the top of the rectifying tower (106) cools tail condensation gas to-45 ℃ through ammonia vacuum evaporation, and qualified industrial-grade or food-grade liquid CO is extracted from the tower kettle of the rectifying tower (106)2And (5) producing the product. Then sent to a subcooler (107) through a product pipeline (6), subcooled to minus 25 ℃ through ammonia evaporation refrigeration, and then sent to a product storage tank through a product pipeline (7). The invention has clear process flow, low working pressure and low equipment manufacturing difficulty, improves the refrigeration coefficient of a refrigeration system, and simultaneously improves CO2The system yield can achieve the purposes of energy saving and consumption reduction.
Further, the raw material gas after drying and dehydration was controlled to 3.3MPa, 38 ℃.
Further, a first residual cold recoverer (101) and a second residual cold recoverer (102) are adopted to recover residual cold of the non-condensable gas, specifically, the non-condensable gas from a rectifying tower (106) firstly enters the second residual cold recoverer (102) to recover the residual cold to 0 ℃, then is decompressed to 0.15MPa and 17 ℃ through a rectifying tower pressure control valve (F1), then enters the first residual cold recoverer (101), recovers the non-condensable gas residual cold to 28 ℃, and finally is discharged through a non-condensable gas pipeline. Aims to avoid the direct decompression of high-pressure and low-temperature noncondensable gas to generate dry ice to block a pipeline and two residual cold recoverers.
Further, the non-condensable gas in the rectifying tower (106) is controlled to be 3.3MPa and 45 ℃ below zero.
Further, a rectifying tower (106) and an economizer (103) are adopted for supercooling the refrigerant, specifically, liquid ammonia from an ammonia storage device is directly connected to a reboiler of a tower kettle of the rectifying tower (106) through a liquid ammonia pipeline (A) and is connected with liquid CO in the tower kettle of the rectifying tower2The heat supply is reboiled, the self is supercooled to 8 ℃, then the cooled heat is sent to an economizer (103) and is further supercooled to-18 ℃ through ammonia evaporation refrigeration, and finally the cooled heat is sent to subsequent refrigeration equipment through a liquid ammonia pipeline (E). The liquid ammonia as refrigerant is firstly used as heat source medium to supply heat to the reboiler of the tower kettle of the rectifying tower (106), and then is subcooled, and then is further subcooled by the economizer (103) so as to improve the refrigerating efficiency of the refrigerating system of the whole ice machine and achieve the purposes of saving energy and reducing consumptionThe refrigerant is used as a heat source medium, no external heat is added, and not only is the utility investment saved, but also the refrigerant is supercooled.
Further, the liquid ammonia in the ammonia storage tank was controlled at 35 ℃ and 1.3 MPa.
Further, in the grading refrigeration process of the refrigeration system, the grading refrigeration corresponds to multi-stage liquefaction,
a primary refrigeration process: in order to make the cooled material reach-18 ℃, liquid ammonia from a liquid ammonia pipeline (B) passes through a liquid ammonia pipeline (D), is decompressed to-24 ℃ through an economizer decompression valve (F2) and is subjected to evaporative refrigeration in an economizer (103), the other part of liquid ammonia from a liquid ammonia pipeline (E) with the pressure of-18 ℃ and the pressure of 1.3MPa is decompressed to-24 ℃ through a liquid ammonia pipeline (I) through a primary condenser decompression valve (F3) and is subjected to evaporative refrigeration in a primary condenser (104), ammonia vapor with the temperature of-18 ℃ generated by the economizer (103) and the primary condenser (104) is led out through a gas ammonia pipeline (L) and a gas ammonia pipeline (M) in sequence and then is converged into a gas ammonia pipeline (Q) and is sent to a primary refrigeration ice maker (108).
And (3) secondary refrigeration process: in order to enable the cooled material to reach the temperature of-25 ℃, liquid ammonia from a liquid ammonia pipeline (E) respectively passes through a liquid ammonia pipeline (J) and a liquid ammonia pipeline (F), then sequentially passes through a secondary condenser pressure reducing valve (F4) and a subcooler pressure reducing valve (F5) to be reduced to-31 ℃, is evaporated and refrigerated in a secondary condenser (105) and a subcooler (107), ammonia vapor generated by evaporation is respectively led out through a gas ammonia pipeline (N) and a gas ammonia pipeline (O), then is converged into a gas ammonia pipeline (R), and then is sent to a secondary refrigeration ice maker (109).
And (3) a three-stage refrigeration process: in order to make the cooled material reach the temperature of minus 45 ℃, liquid ammonia from a liquid ammonia pipeline (E) passes through a liquid ammonia pipeline (K), is subjected to vacuum pressure reduction to minus 51 ℃ through a pressure reducing valve (F6) of a tail condenser of the rectifying tower, is evaporated and refrigerated in the tail condenser of the rectifying tower (106), and generated ammonia steam is led out through a pipeline (P) and then is sent into a three-stage refrigeration ice maker (110).
Gas ammonia with the pressure of 1.3MPa and the temperature of 65 ℃ from a first-stage refrigeration ice machine (108), a second-stage refrigeration ice machine (109) and a third-stage refrigeration ice machine (110) is respectively led out through a gas ammonia pipeline (S), a gas ammonia pipeline (T) and a gas ammonia pipeline (U), then is converged into a gas ammonia pipeline (V) and is sent into an evaporative condenser for condensation.
The inventionThe technological process adopts a multistage liquefaction corresponding grading refrigeration process, greatly improves the thermal cycle efficiency and the refrigeration coefficient of a refrigeration system, reduces the energy consumption of the system, and ensures that each ton of liquid CO is subjected to heat treatment2The energy consumption of the product is 163-188 kW.h (raw material gas CO)2The higher the concentration is, the lower the energy consumption is), and the energy consumption per ton of products in the prior art is 200-220 kW.h.
Further, in the primary refrigeration process, the liquid ammonia of the liquid ammonia pipeline (B) is controlled to be 1.3MPa and 8 ℃; in the secondary refrigeration process, controlling the liquid ammonia in the liquid ammonia pipeline (E) to be 1.3MPa and 18 ℃ below zero; in the three-stage refrigeration process, the liquid ammonia in the liquid ammonia pipeline (E) is controlled to be 1.3MPa and 18 ℃ below zero.
Further, qualified industrial grade or food grade liquid CO2The specific steps of sending the product to the product storage tank through the product pipeline (7) are as follows:
1) the placing racks are fixed on poured concrete through bolts, the distance between every two adjacent placing racks is controlled, the distance is designed by taking out a product storage tank, a sliding guide rail is welded in a notch of each placing rack, and the top surface of the sliding guide rail is lower than that of the notch. The placing rack is arranged on the concrete, and is mainly used for enabling qualified industrial grade or food grade liquid CO to be qualified2The product collection is operated in the inner space of the placing rack, and firstly, the product storage tank can be increased to collect qualified industrial-grade or food-grade liquid CO2The product storage tanks can be properly protected, and the product storage tanks can be orderly arranged and the distance between two adjacent product storage tanks can be controlled.
2) And horizontally placing the product storage tank in the groove of the base, fixing a hoop plate on the base, and horizontally fixing the product storage tank by the hoop plate and the base to form a product storage unit. The clamp plate and the base can keep the product storage tank in a horizontal state, and the product storage tank is convenient to move.
3) Place product storage unit one by one on the guide rail that slides between two adjacent racks, slide product storage unit into the rack again, the base is spacing in the notch of rack for the power that product storage unit received can share on the rack.
4) And two opposite-top fixing rods are respectively in threaded connection with the centering support, the distance between the two opposite-top fixing rods is adjusted to the maximum distance, then the pipeline clamping plate is placed between the two opposite-top fixing rods, and meanwhile, the opposite-top fixing rods are twisted to fix the end parts of the opposite-top fixing rods on the pipeline clamping plate. The horizontal position of the pipeline clamping plate can be changed by respectively adjusting the opposite top fixing rods on the centering supports.
5) The sleeve of the centering support is slid onto the threaded rod of the placing frame, the nut is screwed into the threaded rod, the centering support is fixed on the placing frame, the connecting pipe is screwed into one of the pipeline holes of the pipeline clamping plate through threads, the position of the product storage unit in the placing frame is adjusted simultaneously, the connecting pipe is correspondingly connected with the interface of the product storage tank, the connecting pipe is screwed into the residual pipeline holes of the pipeline clamping plate, and the connecting pipe is correspondingly connected with the residual interface of the product storage tank. Because the direct interface connection with product pipeline (7) and product storage tank can lead to junction sepage phenomenon, consequently add the connecting pipe, as the linking effect of product pipeline (7) and product storage tank, play the supporting role to the connecting pipe through the centering support simultaneously, the power that the connecting pipe received is shared on the rack, increases the stability of connecting pipe, has the effect of shock attenuation, noise reduction.
6) Connecting the product pipeline (7) with a connecting pipe, and connecting qualified industrial grade or food grade liquid CO2The product is sent to the product storage tank through a product pipeline (7) and a connecting pipe in sequence.
7) When the product storage tank is full of qualified industrial grade or food grade liquid CO2During the product, throw off product pipeline (7) from the connecting pipe, twist the connecting pipe again, throw off the kneck of connecting pipe from the product storage tank, then slide product storage unit on the guide rail that slides, slide product storage unit to the region between two adjacent racks, demolish the hoop board on the base, take out the product storage tank, then adopt the transport vechicle to deliver to the factory storehouse with the product storage tank and deposit. Sufficient space is provided between two adjacent placing racks, so that the product storage tank is convenient to take out.
Further, in the step 7), firstly, a binding rope is arranged on the product storage tank, then the binding rope is arranged on a lifting hook of the crane, the product storage tank is taken out and lifted onto a transport vehicle, and the product storage tank is conveniently conveyed in a centralized mode.
Due to the adoption of the technical scheme, the invention has the following beneficial effects:
1. the invention comprises a first residual cold recoverer (101), a second residual cold recoverer (102), a primary condenser (104), a secondary condenser (105), a rectifying tower (106) and a subcooler (107); feed gas pipelines (1, 2, 3); raw material gas-liquid mixing pipelines (4, 5); product conduits (6, 7). The feed gas is liquefied in multiple stages, and the refrigeration mode of the refrigeration system is changed, so that the staged refrigeration of the refrigeration system is realized, the refrigeration coefficient of the refrigeration system is improved, and the CO is improved at the same time2The system yield can achieve the purposes of energy saving and consumption reduction.
2. The invention adopts the non-condensable gas waste cold recovery technology, which comprises a first waste cold recovery device (101), a second waste cold recovery device (102), a rectifying tower pressure control valve (F1) and non-condensable gas pipelines (8, 9, 10 and 11). The double residual cold recovery is to recover partial residual cold of the non-condensable gas firstly, heat the non-condensable gas back and forth, and then reduce the pressure to recover the residual cold, and the aim is to avoid the direct pressure reduction of the non-condensable gas with high pressure and low temperature to generate dry ice to block a pipeline and a residual cold recoverer.
3. The invention adopts a refrigerant supercooling technology, and comprises a rectifying tower (106), an economizer (103) and a liquid ammonia pipeline (A, B, C, E). The liquid ammonia as a refrigerant is firstly used as a heat source medium to supply heat to a reboiler at the tower bottom of the rectifying tower (106), is subcooled, and then is further subcooled by the economizer (103) so as to improve the refrigeration efficiency of the whole ice machine refrigeration system and achieve the purposes of energy saving and consumption reduction.
4. The invention adopts a grading refrigeration technology, which comprises an economizer (103), a first-stage condenser (104), a second-stage condenser (105), a rectifying tower (106), a first-stage refrigeration ice machine (108), a second-stage refrigeration ice machine (109) and a third-stage refrigeration ice machine (110); a liquid ammonia conduit (D, F, I, J, K); a gas ammonia conduit (L, M, N, O, P, Q, R, S, T, U, V); an economizer ammonia pressure reducing valve (F2), a primary condenser pressure reducing valve (F3), a secondary condenser pressure reducing valve (F4), a subcooler ammonia pressure reducing valve (F5) and a rectifying tower tailing condenser ammonia pressure reducing valve (F6). Grading refrigeration is correspondingly carried out, liquefaction is carried out, the refrigeration system of the ice machine is divided into three refrigeration temperature (the temperature of the cooled material needs to be reached) grades of (-18 ℃), -25 ℃ and (-45 ℃), and three refrigeration ice machines with corresponding refrigeration temperatures (the corresponding ammonia evaporation temperatures of (-24 ℃), -31 ℃) and, -51 ℃) are arranged, so that the refrigeration coefficient and the heat cycle efficiency of the refrigeration system of the ice machine are improved, and the purposes of saving energy and reducing consumption are achieved.
5. Among the prior art, the independent level of product storage tank is placed, does not have the restraint to the product storage tank, easily causes the product pipeline that connects between the product storage tank to influence each other, is difficult for setting up the binding rope at the product storage tank moreover and hangs and put easily also easily causing the product pipeline that causes to connect between the product storage tank.
Aiming at the situation, the invention leads qualified industrial grade or food grade liquid CO to be2The product collection is operated in the inner space of the placing rack, and firstly, the product storage tank can be increased to collect qualified industrial-grade or food-grade liquid CO2Stability of (2); secondly, the product storage tank can be protected properly; and thirdly, the product storage tanks can be orderly arranged, and the distance between two adjacent product storage tanks is controlled. When the product storage tank is full of qualified industrial grade or food grade liquid CO2During the product, can slide product storage unit on the guide rail that slides, slide product storage unit to the region between two adjacent racks, demolish the hoop board on the base, take out the product storage tank, switch over the operating condition of product storage tank through the inner space of rack and the region between two adjacent racks like this, conveniently to qualified industrial grade or food level liquid CO2And (4) storing the product. Because the direct interface connection with product pipeline (7) and product storage tank can lead to junction sepage phenomenon, consequently add the connecting pipe, as the linking effect of product pipeline (7) and product storage tank, play the supporting role to the connecting pipe through the centering support simultaneously, the power that the connecting pipe received is shared on the rack, increase the stability of connecting pipe, the shock attenuation has, the effect of noise reduction, also enable product pipeline (7) to distribute in order, and the centering support is spacing on the rack, the connecting pipe is spacing on the pipe grip block, and the product storage tank receives the connection of connecting pipe spacing, make the product pipeline (7) spacingThe storage tank is limited in the placement rack, and the product storage tank is prevented from moving. Finally, because the product storage tank is placed on the base, the product storage tank and the ground have a large operation space, the product storage tank is convenient to arrange a binding rope on the product storage tank, the binding rope is arranged on a lifting hook of a crane, the product storage tank is taken out and lifted onto a transport vehicle, and the product storage tank is convenient to convey in a centralized mode.
Drawings
The invention will be further described with reference to the accompanying drawings in which:
FIG. 1 is a flow chart of a method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas according to the present invention;
FIG. 2 is a schematic structural view of the present invention in the process of welding the sliding guide rail in the notch of the placing rack;
FIG. 3 is a schematic diagram of a product storage unit according to the present invention;
FIG. 4 is a schematic view of the present invention in a configuration in which the product storage unit is slid into the placement frame;
FIG. 5 is a schematic view of the present invention in a configuration for securing the ends of opposing retaining rods to a tube gripping plate;
FIG. 6 is a schematic view of the present invention in a configuration in which the connection pipe is connected to the interface of the product tank;
FIG. 7 is a schematic view of the present invention in a configuration for removal of the product tank.
In the figure, 1-raw gas pipeline; 2-a feed gas pipeline; 3-a feed gas pipeline; 4-raw gas-liquid mixing pipeline; 5-raw gas-liquid mixing pipeline; 6-a product pipeline; 7-a product conduit; 8-noncondensable gas pipeline; 9-noncondensable gas pipeline; 10-noncondensable gas pipeline; 11-noncondensable gas pipeline; 101-a first residual cold recoverer; 102-a second residual cold recoverer; 103-an economizer; 104-a first-stage condenser; 105-a secondary condenser; 106-a rectifying tower; 107-a subcooler; 108-first stage ice refrigeration machine; 109-secondary refrigeration ice machine; 110-three-stage refrigeration ice machine; a-a liquid ammonia pipeline; b-a liquid ammonia pipeline; a C-liquid ammonia pipeline; a D-liquid ammonia pipeline; an E-liquid ammonia pipeline; an F-liquid ammonia pipeline; i-a liquid ammonia pipeline; a J-liquid ammonia conduit; a K-liquid ammonia pipeline; an L-gas ammonia conduit; an M-gas ammonia conduit; an N-gas ammonia pipeline; an O-gas ammonia conduit; a P-gas ammonia pipeline; q-a gaseous ammonia conduit; r-a gas ammonia conduit; s-a gas ammonia pipeline; a T-gas ammonia conduit; a U-gas ammonia conduit; v-a gas ammonia pipeline; f1-rectifying column pressure control valve; f2-economizer ammonia pressure relief valve; f3 — first stage condenser pressure relief valve; f4-two stage condenser pressure relief valve; f5-subcooler pressure relief valve; f6-ammonia pressure reducing valve of the distillation column tail condenser; 201-placing a rack; 202-a glide rail; 203-threaded rod; 204-a base; 205-a hoop plate; 206-a product storage unit; 207-a tube gripping plate; 208-a cannula; 209-opposite top fixing rods; 210-centering the stent; 211-pipe holes; 212-connecting tube; 213-product tank.
Detailed Description
As shown in fig. 1, the method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas according to the present invention includes a first residual cold recoverer 101, a second residual cold recoverer 102, a first-stage condenser 104, a second-stage condenser 105, a rectifying tower 106, and a subcooler 107; a raw material gas pipeline 1, a raw material gas pipeline 2 and a raw material gas pipeline 3; a raw material gas-liquid mixing pipeline 4 and a raw material gas-liquid mixing pipeline 5; a product conduit 6, a product conduit 7.
The method comprises the following specific steps: the dried and dehydrated feed gas with the pressure of 3.3MPa and the temperature of 38 ℃ enters a first residual cooling recoverer 101 through a feed gas pipeline 1, is pre-cooled to 22 ℃ through heat exchange with non-condensable gas, then enters a second residual cooling recoverer 102 through a feed gas pipeline 2, and is pre-cooled to 16 ℃ through heat exchange with the non-condensable gas. Then the refrigeration system carries out stage refrigeration, the refrigerant is sent to a first-stage condenser 104 through a raw material gas pipeline 3, is cooled to-18 ℃ through ammonia evaporation refrigeration, is sent to a second-stage condenser 105 through a raw material gas-liquid mixing pipeline 4, and is cooled to-25 ℃ through ammonia evaporation refrigeration again. Then the gas enters a rectifying tower 106 through a raw gas-liquid mixing pipeline 5 for rectification and purification, a tail condenser arranged at the top of the rectifying tower 106 cools tail condensation gas to-45 ℃ through ammonia vacuum evaporation, so that qualified industrial grade or food grade liquid CO is extracted from the tower bottom of the rectifying tower 1062And (5) producing the product. Then sent to a subcooler 107 through a product pipeline 6, subcooled to-25 ℃ through ammonia evaporation refrigeration, and then sent to a product storage tank through a product pipeline 7. The invention changes the refrigeration mode of the refrigeration system by adopting multi-stage liquefaction to the feed gas, thereby realizing the stage refrigeration of the refrigeration system and improving the refrigeration coefficient of the refrigeration systemWhile increasing CO2The system yield is high, the purposes of energy conservation and consumption reduction are achieved, the process flow is clear in level, the working pressure is low, and the equipment manufacturing difficulty is low.
The non-condensable gas waste cold recovery technology is adopted and comprises a first waste cold recovery device 101, a second waste cold recovery device 102, a rectifying tower pressure control valve F1, a non-condensable gas pipeline 8, a non-condensable gas pipeline 9, a non-condensable gas pipeline 10 and a non-condensable gas pipeline 11. The double residual cold recovery is to recover partial residual cold of the non-condensable gas firstly, heat the non-condensable gas back and forth, and then reduce pressure to recover the residual cold.
The method comprises the following specific steps: 3.3 MPa-45 ℃ non-condensable gas from the rectifying tower 106 firstly enters a second residual cold recoverer 102 to recover residual cold to 0 ℃, then is decompressed to 0.15 MPa-17 ℃ through a rectifying tower pressure control valve F1, then enters a first residual cold recoverer 101, recovers the non-condensable gas residual cold again to 28 ℃, and finally is discharged through a non-condensable gas pipeline. The purpose is to avoid the direct decompression of high-pressure and low-temperature noncondensable gas to generate dry ice to block a pipeline and a residual cold recoverer.
Adopts a refrigerant supercooling technology, and comprises a rectifying tower 106, an economizer 103, a liquid ammonia pipeline A, a liquid ammonia pipeline B, a liquid ammonia pipeline C and a liquid ammonia pipeline E. The liquid ammonia as the refrigerant is firstly used as the heat source medium to supply heat to the reboiler at the tower bottom of the rectifying tower 106, is subcooled, and then is further subcooled by the economizer 103, so that the refrigerating efficiency of the refrigerating system of the whole ice machine is improved, and the purposes of saving energy and reducing consumption are achieved.
The method comprises the following specific steps: liquid ammonia from the ammonia storage device at 35 ℃ and 1.3MPa is directly connected with a reboiler at the bottom of the rectifying tower 106 through a liquid ammonia pipeline A and is connected with liquid CO in the bottom of the rectifying tower2The heat supply is reboiled, the self is supercooled to 8 ℃, then the cooled liquid is sent to the economizer 103 to be further supercooled to-18 ℃ through ammonia evaporation refrigeration, and finally the liquid ammonia is sent to subsequent refrigeration equipment through a liquid ammonia pipeline E. Increase CO2The yield can reach 91.5 percent at most and 88.5 percent at least, compared with the CO in the prior art2The recovery increased by approximately 15 percentage points.
The invention adopts a grading refrigeration technology, which comprises an economizer 103, a first-stage condenser 104, a second-stage condenser 105, a rectifying tower 106, a first-stage ice refrigerating machine 108, a second-stage ice refrigerating machine 109 and a third-stage ice refrigerating machine 110; a liquid ammonia pipeline D, a liquid ammonia pipeline F, a liquid ammonia pipeline I, a liquid ammonia pipeline J and a liquid ammonia pipeline K; a gas ammonia pipeline L, a gas ammonia pipeline M, a gas ammonia pipeline N, a gas ammonia pipeline O, a gas ammonia pipeline P, a gas ammonia pipeline Q, a gas ammonia pipeline R, a gas ammonia pipeline S, a gas ammonia pipeline T, a gas ammonia pipeline U and a gas ammonia pipeline V; an economizer ammonia pressure reducing valve F2, a primary condenser pressure reducing valve F3, a secondary condenser pressure reducing valve F4, a subcooler ammonia pressure reducing valve F5, and a rectifier tail condenser ammonia pressure reducing valve F6. The grading refrigeration is correspondingly increased and liquefaction is carried out, the refrigeration system of the ice machine is divided into three refrigeration temperature refrigerated materials with the refrigeration temperature of-18 ℃, 25 ℃ and-45 ℃, and the corresponding ammonia evaporation temperatures of the refrigeration ice machines with the three types of corresponding refrigeration temperatures are-24 ℃, 31 ℃ and 51 ℃ in sequence, so that the refrigeration coefficient and the heat cycle efficiency of the refrigeration system of the ice machine are improved, and the purposes of saving energy and reducing consumption are achieved. The method comprises the following specific steps:
a primary refrigeration process: in order to make the cooled material reach the temperature of-18 ℃, liquid ammonia with the pressure of 1.3MPa and the temperature of 8 ℃ from a liquid ammonia pipeline B passes through a liquid ammonia pipeline D, is decompressed to-24 ℃ through an economizer decompression valve F2, is evaporated and refrigerated in an economizer 103, the other part of liquid ammonia with the pressure of-18 ℃ and the pressure of 1.3MPa from a liquid ammonia pipeline E passes through a liquid ammonia pipeline I, is decompressed to-24 ℃ through a primary condenser decompression valve F3, is evaporated and refrigerated in a primary condenser 104, ammonia vapor with the temperature of-18 ℃ generated by the economizer 103 and the primary condenser 104 is led out through a gas ammonia pipeline L and a gas ammonia pipeline M in sequence, then is converged into a gas ammonia pipeline Q, and is sent to a primary refrigerating.
And (3) secondary refrigeration process: in order to make the cooled material reach the temperature of-25 ℃, liquid ammonia with the pressure of 1.3MPa and-18 ℃ from a liquid ammonia pipeline E respectively passes through a liquid ammonia pipeline J and a liquid ammonia pipeline F, then sequentially passes through a secondary condenser pressure reducing valve F4 and a subcooler pressure reducing valve F5 respectively, is reduced to-31 ℃, is evaporated and refrigerated in a secondary condenser 105 and a subcooler 107 respectively, and ammonia vapor generated by evaporation is led out through a gas ammonia pipeline N and a gas ammonia pipeline O respectively and then is converged into a gas ammonia pipeline R to enter a secondary refrigeration ice maker 109.
And (3) a three-stage refrigeration process: in order to make the cooled material reach the temperature of minus 45 ℃, liquid ammonia at minus 18 ℃ and 1.3MPa from a liquid ammonia pipeline E passes through a liquid ammonia pipeline K and is decompressed to minus 51 ℃ in vacuum through a pressure reducing valve F6 of a tail condenser of the rectifying tower, the liquid ammonia is evaporated and refrigerated in the tail condenser of the rectifying tower 106, and the generated ammonia steam is led out through a pipeline P and then sent into a three-stage ice refrigerating machine 110.
Gas ammonia of 1.3MPa and 65 ℃ from the first-stage ice refrigerator 108, the second-stage ice refrigerator 109 and the third-stage ice refrigerator 110 is respectively led out through a gas ammonia pipeline S, a gas ammonia pipeline T and a gas ammonia pipeline U, then is converged into a gas ammonia pipeline V, and is sent into an evaporative condenser for condensation.
The technological process of the invention adopts a multi-stage liquefaction corresponding grading refrigeration process, greatly improves the thermal cycle efficiency and the refrigeration coefficient of a refrigeration system, reduces the energy consumption of the system, and ensures that each ton of liquid CO is used2The energy consumption of the product is 163-188 kW.h raw material gas CO2The higher the concentration is, the lower the energy consumption is, and the energy consumption per ton of products in the prior art is 200-220 kW.h.
As shown in fig. 2 to 7, qualified industrial-grade or food-grade liquid CO is mixed with2The specific steps of sending the product to the product storage tank 213 through the product conduit 7 are:
1) the placing frames 201 are fixed on the poured concrete by bolts, and the distance between two adjacent placing frames 201 is controlled, and the distance is designed to be able to take out the product storage tank 213. And then a sliding guide rail 202 is welded in the notch of the placing rack 201, and the top surface of the sliding guide rail 202 is lower than the top surface of the notch. The placing rack 201 is arranged on the concrete, and is mainly used for enabling qualified industrial grade or food grade liquid CO to be qualified2The product collection is operated in the inner space of the placing rack 201, and firstly, the product storage tank 213 can be added to collect qualified industrial-grade or food-grade liquid CO2The stability of (2) can be properly protected for the product tanks 213, and (iii) the product tanks 213 can be orderly arranged and the distance between two adjacent product tanks 213 can be controlled.
2) The product storage tank 213 is horizontally positioned in a recess in the base 204, and then the hoop plate 205 is secured to the base 204, with the hoop plate 205 and the base 204 securing the product storage tank 213 horizontally to form the product storage unit 206. Hoop plate 205 and base 204 can maintain product tank 213 horizontal to facilitate movement of product tank 213.
3) The product storage units 206 are placed on the sliding guide rails 202 between the two adjacent placing frames 201 one by one, then the product storage units 206 slide into the placing frames 201, and the base 204 is limited in the notches of the placing frames 201, so that the force applied to the product storage units 206 can be shared on the placing frames 201.
4) Two opposite-top fixing rods 209 are respectively connected to the centering support 210 in a threaded mode, the distance between the two opposite-top fixing rods 209 is adjusted to the maximum distance, the pipeline clamping plate 207 is placed between the two opposite-top fixing rods 209, the opposite-top fixing rods 209 are simultaneously screwed, and the end portions of the opposite-top fixing rods 209 are fixed to the pipeline clamping plate 207. The horizontal position of the tube gripping plate 207 may be changed by adjusting the centering rods 209 on the centering brackets 210, respectively.
5) The sleeve 208 of the centering bracket 210 is slid onto the threaded rod 203 of the rack 201, the nut is screwed onto the threaded rod 203, the centering bracket 210 is fixed on the rack 201, the connecting pipe 212 is screwed into one of the pipe holes 211 of the pipe clamping plate 207, and the position of the product storage unit 206 in the rack 201 is adjusted, so that the connecting pipe 212 is correspondingly connected with the interface of the product storage tank 213. Then, the connecting pipe 212 is screwed into the remaining pipe hole 211 of the pipe clamping plate 207, and the connecting pipe 212 and the remaining interface of the product tank 213 are correspondingly connected, so that the situation that the interfaces of the connecting pipe 212 and the product tank 213 cannot be directly connected can be avoided. Because the direct interface connection with product pipeline 7 and product storage tank 213 can lead to junction sepage phenomenon, consequently add connecting pipe 212, as product pipeline 7 and product storage tank 213's linking effect, play the supporting role to connecting pipe 212 through centering support 210 simultaneously, the power that connecting pipe 212 received is shared on rack 201, increases the stability of connecting pipe 212, has the effect of shock attenuation, noise reduction.
6) Connecting the product pipeline 7 with the connecting pipe 212, and connecting qualified industrial grade or food grade liquid CO2The product is passed through product conduit 7 and connecting pipe 212 in sequence to product tank 213.
7) When the product storage tank 213 is full of qualified industrial-grade or food-grade liquid CO2When producing, the product is piped7 are disconnected from the connecting tube 212, the connecting tube 212 is screwed, the connecting tube 212 is disconnected from the interface of the product storage tank 213, then the product storage unit 206 is slid on the sliding guide rail 202, the product storage unit 206 is slid to the area between two adjacent racks 201, the hoop plate 205 is removed from the base 204, the product storage tank 213 is taken out, and then the product storage tank 213 is transported to a factory warehouse for storage by using a transport vehicle. There is sufficient space between two adjacent racks 201 to facilitate removal of the product tank 213.
In step 7), a binding rope is firstly arranged on the product storage tank 213, then the binding rope is arranged on a lifting hook of a crane, the product storage tank 213 is taken out and lifted to a transport vehicle, and the product storage tank 213 is conveniently conveyed in a centralized manner.
Among the prior art, product storage tank 213 is the level alone and places, does not have the restraint to product storage tank 213, easily causes the product pipeline that connects between the product storage tank 213 to influence each other, also easily causes product storage tank 213 to set up the binding rope moreover and hang and put.
Aiming at the situation, the invention leads qualified industrial grade or food grade liquid CO to be2The product collection is operated in the inner space of the placing rack 201, and firstly, the product storage tank 213 can be added to collect qualified industrial-grade or food-grade liquid CO2Stability of (2); secondly, the product storage tank 213 can be protected properly; third, the product tanks 213 can be arranged in order, and the distance between two adjacent product tanks 213 can be controlled. When the product storage tank 213 is full of qualified industrial-grade or food-grade liquid CO2During production, the product storage unit 206 can slide on the sliding guide rail 202, the product storage unit 206 slides to the area between the two adjacent placing frames 201, the hoop plate 205 is detached from the base 204, the product storage tank 213 is taken out, and thus the working state of the product storage tank 213 is switched through the inner space of the placing frames 201 and the area between the two adjacent placing frames 201, and qualified industrial-grade or food-grade liquid CO is convenient to use2And (4) storing the product. Since the direct connection of the product conduit 7 to the product tank 213 will cause seepage at the connection, the connection pipe 212 is added as a connection between the product conduit 7 and the product tank 213During the process, the centering support 210 is used for supporting the connecting pipe 212, the force received by the connecting pipe 212 is shared on the placement frame 201, the stability of the connecting pipe 212 is improved, the damping and noise reduction effects are achieved, the product pipelines 7 can be distributed orderly, the centering support 210 is limited on the placement frame 201, the connecting pipe 212 is limited on the pipeline clamping plate 207, the product storage tank 213 is limited by the connecting pipe 212, the product storage tank 213 is limited in the placement frame 201, and the product storage tank 213 is prevented from moving. Finally, because product storage tank 213 is placed on base 204, product storage tank 213 and the ground have a larger operating space, which is convenient for set binding rope on product storage tank 213, and then set binding rope on the hook of crane, take product storage tank 213 out, and put it on the transport vehicle, which is convenient for centralized transportation of product storage tank 213.
The above is only a specific embodiment of the present invention, but the technical features of the present invention are not limited thereto. Any simple changes, equivalent substitutions or modifications made based on the present invention to solve the same technical problems and achieve the same technical effects are within the scope of the present invention.
Claims (7)
1. A method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas is characterized by comprising the following steps: the dried and dehydrated feed gas firstly enters a first residual cooling recoverer (101) through a feed gas pipeline (1), is pre-cooled to 22 ℃ by exchanging heat with non-condensable gas, then the waste gas is sent to a second waste cold recoverer (102) through a raw gas pipeline (2) and is pre-cooled to 16 ℃ after exchanging heat with non-condensable gas, then the refrigeration system carries out stage refrigeration, the raw material gas is sent to a first-stage condenser (104) through a raw material gas pipeline (3), cooled to-18 ℃ through ammonia evaporation refrigeration, then sent to a secondary condenser (105) through a feed gas-liquid mixing pipeline (4), cooled to-25 ℃ through ammonia evaporation refrigeration again, and then the gas enters a rectifying tower (106) through a raw gas-liquid mixing pipeline (5) for rectification and purification, and a tail condenser arranged at the top of the rectifying tower (106) cools tail condensation gas to-45 ℃ through ammonia vacuum evaporation, so that qualified industrial-grade or food-grade liquid CO is extracted from the tower kettle of the rectifying tower (106).2The product is sent to a subcooler (107) through a product pipeline (6)The ammonia is refrigerated and supercooled to-25 ℃ through ammonia evaporation and then sent to a product storage tank through a product pipeline (7);
the method comprises the following steps of (1) adopting a first residual cold recoverer (101) and a second residual cold recoverer (102) to recover residual cold from non-condensable gas, specifically, enabling the non-condensable gas from a rectifying tower (106) to firstly enter the second residual cold recoverer (102) to recover the residual cold to 0 ℃, then reducing the pressure to 0.15MPa through a rectifying tower pressure control valve (F1), then entering the first residual cold recoverer (101), recovering the non-condensable gas residual cold again to 28 ℃, and finally emptying through a non-condensable gas pipeline;
in the grading refrigeration process of the refrigeration system, grading refrigeration corresponds to multi-stage liquefaction:
a primary refrigeration process: in order to make the cooled material reach the temperature of-18 ℃, liquid ammonia with the pressure of 1.3MPa and the temperature of 8 ℃ from a liquid ammonia pipeline (B) passes through a liquid ammonia pipeline (D), is decompressed to-24 ℃ through an economizer decompression valve (F2) and is evaporated and refrigerated in an economizer (103), the other part of liquid ammonia with the pressure of-18 ℃ and the pressure of 1.3MPa from a liquid ammonia pipeline (E) passes through a liquid ammonia pipeline (I), is decompressed to-24 ℃ through a primary condenser decompression valve (F3) and is evaporated and refrigerated in a primary condenser (104), ammonia vapor with the temperature of-18 ℃ generated by the economizer (103) and the primary condenser (104) is led out through a gas ammonia pipeline (L) and a gas ammonia pipeline (M) in sequence and then is converged into the gas ammonia pipeline (Q) and is sent to a primary refrigeration ice maker (108;
and (3) secondary refrigeration process: in order to enable the cooled material to reach the temperature of-25 ℃, liquid ammonia at the temperature of-18 ℃ and 1.3MPa from a liquid ammonia pipeline (E) respectively passes through a liquid ammonia pipeline (J) and a liquid ammonia pipeline (F), then sequentially passes through a secondary condenser pressure reducing valve (F4) and a subcooler pressure reducing valve (F5) to be reduced to-31 ℃, is respectively evaporated and refrigerated in a secondary condenser (105) and a subcooler (107), and ammonia vapor generated by evaporation is respectively led out through a gas ammonia pipeline (N) and a gas ammonia pipeline (O), then is converged into a gas ammonia pipeline (R) and enters a secondary refrigeration ice maker (109);
and (3) a three-stage refrigeration process: in order to make the cooled material reach the temperature of minus 45 ℃, liquid ammonia at minus 18 ℃ and 1.3MPa from a liquid ammonia pipeline (E) passes through a liquid ammonia pipeline (K) and is subjected to vacuum pressure reduction to minus 51 ℃ through a pressure reducing valve (F6) of a tail condenser of a rectifying tower, evaporation refrigeration is carried out in the tail condenser of the rectifying tower (106), and generated ammonia steam is led out through a pipeline (P) and then sent into a three-stage refrigeration ice maker (110);
gas ammonia with the pressure of 1.3MPa and the temperature of 65 ℃ from a first-stage refrigeration ice machine (108), a second-stage refrigeration ice machine (109) and a third-stage refrigeration ice machine (110) is respectively led out through a gas ammonia pipeline (S), a gas ammonia pipeline (T) and a gas ammonia pipeline (U), then is converged into a gas ammonia pipeline (V) and is sent into an evaporative condenser for condensation.
2. The method for recovering the carbon dioxide by the multistage liquefaction and the fractional refrigeration of the industrial tail gas according to claim 1, characterized by comprising the following steps of: the raw material gas after drying and dehydration is controlled to be 3.3MPa and 38 ℃.
3. The method for recovering the carbon dioxide by the multistage liquefaction and the fractional refrigeration of the industrial tail gas according to claim 1, characterized by comprising the following steps of: the non-condensable gas of the rectifying tower (106) is controlled to be 3.3MPa and minus 45 ℃.
4. The method for recovering the carbon dioxide by the multistage liquefaction and the fractional refrigeration of the industrial tail gas according to claim 1, characterized by comprising the following steps of: adopts a rectifying tower (106) and an economizer (103) to carry out refrigerant supercooling, in particular to a method that liquid ammonia from an ammonia storage device is directly connected on a reboiler of a tower kettle of the rectifying tower (106) through a liquid ammonia pipeline (A) and is connected with liquid CO in the tower kettle of the rectifying tower2The heat supply is reboiled, the self is supercooled to 8 ℃, then the cooled heat is sent to an economizer (103) and is further supercooled to-18 ℃ through ammonia evaporation refrigeration, and finally the cooled heat is sent to subsequent refrigeration equipment through a liquid ammonia pipeline (E).
5. The method for recovering the carbon dioxide by the multistage liquefaction and the fractional refrigeration of the industrial tail gas according to claim 4, characterized by comprising the following steps of: the liquid ammonia in the ammonia storage device is controlled at 35 ℃ and 1.3 MPa.
6. The method for recovering the carbon dioxide by the multistage liquefaction and the fractional refrigeration of the industrial tail gas as claimed in claim 1, wherein qualified industrial-grade or food-grade liquid CO is recycled2The specific steps of sending the product to the product storage tank through the product pipeline (7) are as follows:
1) fixing the placing racks on the poured concrete through bolts, controlling the distance between every two adjacent placing racks, designing the distance so as to be capable of taking out the product storage tank, and welding a sliding guide rail in a notch of each placing rack, wherein the top surface of the sliding guide rail is lower than that of the notch;
2) horizontally placing the product storage tank in the groove of the base, fixing a hoop plate on the base, and horizontally fixing the product storage tank by the hoop plate and the base to form a product storage unit;
3) placing the product storage units one by one on a sliding guide rail between two adjacent placing racks, sliding the product storage units into the placing racks, and limiting the base in a notch of the placing racks;
4) the centering support is respectively in threaded connection with two opposite-top fixing rods, the distance between the two opposite-top fixing rods is adjusted to the maximum distance, then the pipeline clamping plate is placed between the two opposite-top fixing rods, the opposite-top fixing rods are simultaneously screwed, and the end parts of the opposite-top fixing rods are fixed on the pipeline clamping plate;
5) sliding a sleeve of the centering support onto a threaded rod of the placing frame, screwing a nut on the threaded rod, fixing the centering support on the placing frame, screwing a connecting pipe into one of the pipeline holes of the pipeline clamping plate in a threaded manner, adjusting the position of a product storage unit in the placing frame simultaneously to enable the connecting pipe to be correspondingly connected with an interface of a product storage tank, screwing connecting pipes into the rest pipeline holes of the pipeline clamping plate, and correspondingly connecting the connecting pipes with the rest interfaces of the product storage tank;
6) connecting the product pipeline (7) with a connecting pipe, and connecting qualified industrial grade or food grade liquid CO2The product is sent to a product storage tank through a product pipeline (7) and a connecting pipe in sequence;
7) when the product storage tank is full of qualified industrial grade or food grade liquid CO2During the product, throw off product pipeline (7) from the connecting pipe, twist the connecting pipe again, throw off the kneck of connecting pipe from the product storage tank, then slide product storage unit on the guide rail that slides, slide product storage unit to the region between two adjacent racks, demolish the hoop board on the base, take out the product storage tank, then adopt the transport vechicle to deliver to the factory storehouse with the product storage tank and deposit.
7. The method for recovering the carbon dioxide by the multistage liquefaction and the staged refrigeration of the industrial tail gas as claimed in claim 6, wherein the method comprises the following steps: in the step 7), firstly, a binding rope is arranged on the product storage tank, then the binding rope is arranged on a lifting hook of a crane, and the product storage tank is taken out and lifted to a transport vehicle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911094021.3A CN110801639B (en) | 2019-11-11 | 2019-11-11 | Method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911094021.3A CN110801639B (en) | 2019-11-11 | 2019-11-11 | Method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110801639A CN110801639A (en) | 2020-02-18 |
| CN110801639B true CN110801639B (en) | 2021-06-01 |
Family
ID=69501811
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911094021.3A Active CN110801639B (en) | 2019-11-11 | 2019-11-11 | Method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110801639B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114485051B (en) * | 2022-01-24 | 2023-06-20 | 广州市华达石化有限公司 | Liquid ammonia double-working-condition refrigerating system and liquid carbon dioxide production equipment |
| CN116036632A (en) * | 2023-01-10 | 2023-05-02 | 杭州快凯高效节能新技术有限公司 | A high-purity carbon dioxide preparation system and its preparation process |
| CN119268439B (en) * | 2024-12-09 | 2025-02-25 | 中太海碳(上海)环保科技有限公司 | Heat exchange system for precooling carbon dioxide by liquid ammonia and control method |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3349571A (en) * | 1966-01-14 | 1967-10-31 | Chemical Construction Corp | Removal of carbon dioxide from synthesis gas using spearated products to cool external refrigeration cycle |
| US3817046A (en) * | 1970-11-28 | 1974-06-18 | Chinzoda Chem Eng & Constructi | Absorption-multicomponent cascade refrigeration for multi-level cooling of gas mixtures |
| US3954430A (en) * | 1974-10-30 | 1976-05-04 | Ppg Industries, Inc. | Liquefaction of chlorine by multi-stage compression and cooling |
| US6301927B1 (en) * | 1998-01-08 | 2001-10-16 | Satish Reddy | Autorefrigeration separation of carbon dioxide |
| CN1476346A (en) * | 2001-01-30 | 2004-02-18 | Method and system for extracting and storing carbon dioxide by desublimation | |
| CN1816497A (en) * | 2003-05-07 | 2006-08-09 | 普莱克斯技术有限公司 | Process for carbon dioxide recovery |
| CN101434507A (en) * | 2008-11-19 | 2009-05-20 | 上海惠生化工工程有限公司 | Separation method for fischer-tropsch synthesis tail gas |
| KR20100124547A (en) * | 2009-05-19 | 2010-11-29 | 대우조선해양 주식회사 | Treatability and system of the carbon dioxide which occurs from the vessel which is in the process of operating |
| CN101952003A (en) * | 2007-03-06 | 2011-01-19 | 林德股份公司 | Separation method |
| CN103687659A (en) * | 2011-07-11 | 2014-03-26 | 阿尔斯通技术有限公司 | Thermal Comprehensive Utilization for Low Temperature Carbon Dioxide Separation |
| CN105263605A (en) * | 2013-06-10 | 2016-01-20 | 株式会社Ihi | Impurities removal system |
| CN108043064A (en) * | 2017-12-29 | 2018-05-18 | 上海蓝科石化环保科技股份有限公司 | A kind of VOCs recovery process and system |
Family Cites Families (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL127840C (en) * | 1963-08-17 | |||
| US3362173A (en) * | 1965-02-16 | 1968-01-09 | Lummus Co | Liquefaction process employing cascade refrigeration |
| JPS5371103A (en) * | 1976-12-04 | 1978-06-24 | Nisshin Steel Co Ltd | Method of increasing calorie of fuel gas |
| RU2023387C1 (en) * | 1991-06-28 | 1994-11-30 | Рашид Зарифович Аминов | Method of supply of hothouse with thermal energy and carbon dioxide |
| DE4402499C1 (en) * | 1994-01-28 | 1995-04-27 | Boewe Passat Reinigung | Process and apparatus for distilling a contaminated hydrocarbon solvent liquor |
| RU2352877C2 (en) * | 2003-09-23 | 2009-04-20 | Статойл Аса | Method of liquefying natural gas |
| CN101666573B (en) * | 2009-09-21 | 2011-06-08 | 华北电力大学 | CO2 separation and compression integrated method |
| CN101858685A (en) * | 2010-05-26 | 2010-10-13 | 华北电力大学 | CO2 separation-liquefaction-purification system and method |
| CN102538395A (en) * | 2012-03-05 | 2012-07-04 | 苏州市兴鲁空分设备科技发展有限公司 | Carbon dioxide purification technology |
| CN102974119B (en) * | 2012-12-18 | 2015-04-08 | 华东理工大学 | Gas condensation and grading device and application method thereof |
| CN204134250U (en) * | 2014-09-25 | 2015-02-04 | 青海制药厂有限公司 | The organic waste gas purification recovery device of a kind of mixing |
| CN104896873A (en) * | 2015-06-17 | 2015-09-09 | 镇江索普天辰碳回收有限公司 | Improved integrated food-grade industrial-grade CO2 recovery device and process |
| CN106310877A (en) * | 2016-08-23 | 2017-01-11 | 孙桂菊 | High-efficiency energy-saving volatile-organic-solvent-containing tail gas recovery technique |
| CN206184226U (en) * | 2016-08-25 | 2017-05-24 | 中国神华能源股份有限公司 | Flue gas water trap and carbon dioxide capture system |
| CN108821288B (en) * | 2018-07-03 | 2020-08-07 | 杭州快凯高效节能新技术有限公司 | Preparation device and preparation process for producing high-quality liquid carbon dioxide |
-
2019
- 2019-11-11 CN CN201911094021.3A patent/CN110801639B/en active Active
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3349571A (en) * | 1966-01-14 | 1967-10-31 | Chemical Construction Corp | Removal of carbon dioxide from synthesis gas using spearated products to cool external refrigeration cycle |
| GB1141224A (en) * | 1966-01-14 | 1969-01-29 | Chemical Construction Corp | Cold separation of gas mixtures |
| US3817046A (en) * | 1970-11-28 | 1974-06-18 | Chinzoda Chem Eng & Constructi | Absorption-multicomponent cascade refrigeration for multi-level cooling of gas mixtures |
| US3954430A (en) * | 1974-10-30 | 1976-05-04 | Ppg Industries, Inc. | Liquefaction of chlorine by multi-stage compression and cooling |
| US6301927B1 (en) * | 1998-01-08 | 2001-10-16 | Satish Reddy | Autorefrigeration separation of carbon dioxide |
| CN1476346A (en) * | 2001-01-30 | 2004-02-18 | Method and system for extracting and storing carbon dioxide by desublimation | |
| CN1816497A (en) * | 2003-05-07 | 2006-08-09 | 普莱克斯技术有限公司 | Process for carbon dioxide recovery |
| CN101952003A (en) * | 2007-03-06 | 2011-01-19 | 林德股份公司 | Separation method |
| CN101434507A (en) * | 2008-11-19 | 2009-05-20 | 上海惠生化工工程有限公司 | Separation method for fischer-tropsch synthesis tail gas |
| KR20100124547A (en) * | 2009-05-19 | 2010-11-29 | 대우조선해양 주식회사 | Treatability and system of the carbon dioxide which occurs from the vessel which is in the process of operating |
| CN103687659A (en) * | 2011-07-11 | 2014-03-26 | 阿尔斯通技术有限公司 | Thermal Comprehensive Utilization for Low Temperature Carbon Dioxide Separation |
| CN105263605A (en) * | 2013-06-10 | 2016-01-20 | 株式会社Ihi | Impurities removal system |
| CN108043064A (en) * | 2017-12-29 | 2018-05-18 | 上海蓝科石化环保科技股份有限公司 | A kind of VOCs recovery process and system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110801639A (en) | 2020-02-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110801639B (en) | Method for recovering carbon dioxide by multistage liquefaction and fractional refrigeration of industrial tail gas | |
| CN104807286B (en) | Recycle the nitrogen gas liquefaction system of LNG cold energy | |
| CN101040674B (en) | Method for producing food level liquid carbon dioxide product | |
| CN107606874B (en) | Device for recycling argon through full rectification purification and argon recycling method thereof | |
| CN102538398B (en) | Process and system for purifying, separating and liquefying nitrogen-and-oxygen-containing coal mine methane (CMM) | |
| CN102660341B (en) | Process and device utilizing pressure of natural gas to partially liquefy natural gas | |
| CN1095496C (en) | Process for preparing liquefied natural gas | |
| CN110498416A (en) | A system for synchronous recovery of carbon dioxide and nitrogen from boiler flue gas in a coal-fired power plant | |
| CN104419464B (en) | Dry gas recovery system and dry gas recovery method for refinery plant | |
| CN202595072U (en) | Device for partially liquefying natural gas by using pressure energy of natural gas | |
| CN106402644A (en) | BOG and oil gas combined recycling system of LNG oil gas cooperative station | |
| CN214371298U (en) | Carbon dioxide gathering liquefaction recovery device | |
| CN210832753U (en) | Carbon dioxide compression and purification system of coal-fired boiler | |
| CN114518016A (en) | Carbon dioxide capturing, liquefying and recycling device and method | |
| CN210825439U (en) | A system for synchronously recovering carbon dioxide and nitrogen from boiler flue gas in coal-fired power plants | |
| CN114165987B (en) | Liquid carbon dioxide production device and production method thereof | |
| CN105066586B (en) | Device for preparing raw material gas for synthetic ammonia and L NG by liquid nitrogen washing and preparation method thereof | |
| CN214371300U (en) | High-efficient carbon dioxide condensing equipment | |
| CN203687518U (en) | Low-purity oxygen preparing device with auxiliary rectifying tower | |
| AU2012208462B2 (en) | Installation and method for producing liquid helium | |
| CN209944879U (en) | Process equipment for extracting high-purity carbon dioxide from landfill gas, methane or chemical tail gas | |
| CN106885449B (en) | Utilize the air-separating technology of cold energy of liquefied natural gas | |
| CN103589550A (en) | A carbon dioxide balance system used in beer brewing process | |
| CN116839310A (en) | Process method for preparing food-grade liquid carbon dioxide by utilizing decarburization exhaust gas of LNG (liquefied Natural gas) plant | |
| CN114377513B (en) | Mobile train system and method for recovering and treating oilfield associated gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |