CN111141109B - Heat pump circulation system, carbon monoxide production device with heat pump circulation system and carbon monoxide production method - Google Patents

Heat pump circulation system, carbon monoxide production device with heat pump circulation system and carbon monoxide production method Download PDF

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Publication number
CN111141109B
CN111141109B CN202010153513.1A CN202010153513A CN111141109B CN 111141109 B CN111141109 B CN 111141109B CN 202010153513 A CN202010153513 A CN 202010153513A CN 111141109 B CN111141109 B CN 111141109B
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gas
outlet
liquid
rectifying tower
inlet
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CN111141109A (en
Inventor
李灏
闫红伟
郑梦杰
崔增涛
银延蛟
张亚清
吕书山
郭俊磊
莫佩
杨茂强
樊佳佳
杜兴慧
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Henan Xinlianxin Shenleng Energy Co ltd
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Henan Xinlianxin Shenleng Energy Co ltd
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0261—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon monoxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B30/00—Heat pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B41/00—Fluid-circulation arrangements
    • F25B41/20—Disposition of valves, e.g. of on-off valves or flow control valves
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/14—Carbon monoxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention belongs to a heat pump circulation system, and a carbon monoxide production device and a carbon monoxide production method with the heat pump circulation system. The system comprises a heat pump, wherein a circulating outlet of the heat pump is connected with an inlet of a nitrogen gas-liquid separation tank, a gas phase outlet at the top of the nitrogen gas-liquid separation tank is respectively connected with reboilers at the inner lower parts of a plurality of rectifying towers, a liquid phase outlet at the bottom of the nitrogen gas-liquid separation tank is respectively connected with shell passes of main condensers respectively corresponding to the plurality of rectifying towers through a system cold energy maintaining pipeline, and a shell pass outlet of the main condensers is connected with a circulating inlet of the heat pump; has the characteristics of simple operation, stable operation, low power consumption of unit product and capability of improving the purity of the product to 99.9999 percent of electronic grade.

Description

Heat pump circulation system, carbon monoxide production device with heat pump circulation system and carbon monoxide production method
Technical Field
The invention belongs to the technical field of carbon monoxide production and accessory parts, and particularly relates to a heat pump circulating system, and a carbon monoxide production device and a carbon monoxide production method with the heat pump circulating system.
Background
In the current carbon monoxide production method, the pressure swing adsorption PSA-CO, heat pump rectification and other processes are mainly adopted. The existing PSA-CO process has the following defects: the system occupies large area, has large equipment investment, complex flow and low product purity; the heat pump rectification process has the characteristics of low equipment investment, small occupied area and high product purity, but the existing heat pump rectification process has the defects that the cooling capacity of the top of a rectification tower is insufficient, and the system operation is unstable easily to cause the product purity to fluctuate; in addition, the heat pump nitrogen system has the problems of high energy consumption, incapability of recycling and the like.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide the heat pump circulation system which has the advantages of simple structure, reasonable design, more stable operation of the heat pump rectification process system, low energy consumption and cyclic utilization, and the carbon monoxide production device and the production method with the heat pump circulation system.
In order to achieve the above purpose, the present invention provides the following technical solutions: the heat pump circulation system comprises a heat pump, wherein a circulation outlet of the heat pump is connected with an inlet of a nitrogen gas-liquid separation tank, a gas phase outlet at the top of the nitrogen gas-liquid separation tank is respectively connected with reboilers at the inner lower parts of a plurality of rectifying towers, a liquid phase outlet at the bottom of the nitrogen gas-liquid separation tank is respectively connected with shell passes of main condensers corresponding to the rectifying towers through a system cold maintaining pipeline, and a shell pass outlet of the main condensers is connected with the circulation inlet of the heat pump.
Preferably, first regulating valves are respectively arranged between the reboilers at the lower parts in the plurality of rectifying towers and the gas phase outlets of the nitrogen gas-liquid separation tanks; outlets of reboilers at the lower parts in the rectifying towers are respectively communicated with a system cold maintaining pipeline.
Preferably, the rectifying tower comprises a first rectifying tower and a second rectifying tower; the inner lower part of the first rectifying tower is provided with a first reboiler, and the inner lower part of the second rectifying tower is provided with a second reboiler; the first rectifying tower is correspondingly provided with a first main condenser, and the second rectifying tower is correspondingly provided with a second main condenser.
Preferably, a first tee joint is arranged between the outlet of the reboiler and the system cold energy maintaining pipeline, a second tee joint is arranged between the shell side inlet of the main condenser and the system cold energy maintaining pipeline, and a second regulating valve is arranged on the system cold energy maintaining pipeline between the first tee joint and the second tee joint.
Preferably, a third regulating valve is arranged between the shell side inlet of the main condenser and the second tee joint.
The invention also provides a carbon monoxide production device which comprises a raw material gas storage tank, a product tank, a first rectifying tower, a first reboiler, a first main condenser, a second rectifying tower, a second reboiler, a second main condenser and the heat pump nitrogen circulation system.
Preferably, the raw material gas storage tank is connected with the raw material inlet of the first rectifying tower through the raw material gas inlet of the heat exchanger and the raw material gas outlet of the heat exchanger, the liquid phase outlet at the bottom of the first rectifying tower is connected with the first raw material liquid inlet of the second rectifying tower, the gas phase outlet at the top of the second rectifying tower is connected with the liquid storage tank through the tube pass of the second main condenser, and the liquid phase outlet at the bottom of the liquid storage tank is respectively connected with the product tank and the second raw material liquid inlet at the upper part in the second rectifying tower; the gas phase outlet at the top of the liquid storage tank is connected with the tube side of the second main condenser; the circulating outlet of the heat pump in the nitrogen circulating system of the heat pump is connected with the inlet of the nitrogen gas-liquid separating tank through the first circulating gas inlet of the heat exchanger and the first circulating gas outlet of the heat exchanger; the shell side outlet of the main condenser is connected with the circulating inlet of the heat pump through the second circulating gas inlet of the heat exchanger and the second circulating gas outlet of the heat exchanger.
Preferably, the outlet at the top of the first rectifying tower is connected with a gas-liquid separation tank through the tube pass of the first main condenser, the liquid phase of the gas-liquid separation tank is connected with the liquid inlet at the middle upper part of the first rectifying tower, and the gas phase of the gas-liquid separation tank is connected with the waste gas furnace through the first tail gas inlet of the heat exchanger, the first tail gas outlet of the heat exchanger and the fourth regulating valve; the liquid phase outlet at the bottom of the second rectifying tower is connected with the waste gas furnace through a fifth regulating valve, a second tail gas inlet of the heat exchanger and a second tail gas outlet of the heat exchanger.
Preferably, a sixth regulating valve is arranged between the liquid phase outlet at the bottom of the first rectifying tower and the first raw material liquid inlet of the second rectifying tower; a seventh regulating valve is arranged between the liquid phase outlet at the bottom of the liquid storage tank and the second raw material liquid inlet at the upper part in the second rectifying tower.
The invention also provides a production method of the carbon monoxide production device, which comprises the following steps:
step one: the raw material gas in the raw material gas storage tank 17 sequentially enters the first rectifying tower 7 through the raw material gas inlet 29 of the heat exchanger 19, the raw material gas outlet 30 of the heat exchanger 19 and the raw material inlet of the first rectifying tower 7; the raw material gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: the temperature and pressure are 40 ℃ and are as follows: 0.7MpaG, flow: 2200 Nm/h, a gas phase fraction of 1, carbon monoxide mole fraction: 35%; the feed gas temperature at the feed gas outlet 30 of the heat exchanger 19 is: -163 to-170 ℃ and gas phase fraction of 1;
Step two: the raw material gas entering the first rectifying tower 7 in the first step is subjected to primary rectifying purification, the gas phase after primary rectifying purification enters the gas-liquid separation tank 23 through an outlet at the top of the first rectifying tower 7 and a tube side of the first main condenser 13 to carry out gas-liquid separation, the liquid phase after gas-liquid separation enters the first rectifying tower 7 through the bottom of the gas-liquid separation tank 23 and a liquid inlet at the middle upper part of the first rectifying tower 7 to continue primary rectifying purification, a gas phase outlet of the gas-liquid separation tank 23 enters the waste gas furnace 25 through a first tail gas inlet 35 of the heat exchanger 19, a first tail gas outlet 36 of the heat exchanger 19 and a fourth regulating valve 24, and the gas phase temperature in the gas-liquid separation tank 23 is as follows: -172 to-178 ℃, carbon monoxide mole fraction: 25-30%, gas phase fraction: 1, a step of;
step three: the liquid phase after primary rectification and purification in the first step and the second step sequentially enters the second rectifying tower 8 through a liquid phase outlet at the bottom of the first rectifying tower 7 and a sixth regulating valve 27, secondary rectification and purification are carried out, a gas phase after secondary rectification and purification enters a liquid storage tank 22 through a gas phase outlet at the top of the second rectifying tower 8 and a tube pass of the second main condenser 12, one part of the liquid phase in the liquid storage tank 22 enters the second rectifying tower 8 through a second raw material liquid inlet 21 at the middle and upper part of the second rectifying tower 8, and the other part of the liquid phase enters a product tank 18; the liquid phase temperature of the bottom liquid phase outlet of the first rectifying tower 7 is: -165 to-170 ℃, and the purity of CO is: 69-75%; the product temperature in the product tank 18 is: 172 to 179 ℃ below zero, and the purity is not lower than 99.9999 percent;
Step four: the gas phase of the liquid storage tank 22 in the third step is communicated with the tube side of the second main condenser 12 and enters the tube side of the second main condenser 12 to be condensed;
step five: in the third step, the waste liquid purified by the second rectification column 8 sequentially enters the waste gas furnace 25 through a liquid phase outlet at the bottom of the second rectification column 8, a fifth regulating valve 26, a second tail gas inlet 37 of the heat exchanger 19 and a second tail gas outlet 38 of the heat exchanger 19, and the temperature of the waste liquid at the bottom of the second rectification column 8 is: -166 to-171 ℃, the purity of CO is: 25-30%, gas phase fraction: 0;
step six: the circulating gas in the heat pump 1 sequentially enters the nitrogen gas-liquid separation tank 3 through the circulating outlet 2, the first circulating gas inlet 31 of the heat exchanger 19 and the first circulating gas outlet 32 of the heat exchanger 19, the gas phase outlet of the nitrogen gas-liquid separation tank 3 respectively enters the corresponding first reboiler 9 and second reboiler 10 through two first regulating valves 6, and the components of the circulating gas are as follows: nitrogen, hydrogen, argon, nitrogen mole fraction: 99 percent; the first recycle gas outlet 32 of the heat exchanger 19 has a recycle gas temperature of: -162 to-168 ℃; the temperature of the circulating liquid at the outlet of the first reboiler 9 is as follows: -162 to-168 ℃, gas phase fraction: 0; the temperature of the circulating liquid at the outlet of the second reboiler 10 is: -163 to-170 ℃, gas phase fraction: 0;
Step seven: the liquid phase outlet of the nitrogen gas-liquid separation tank 3 in the step six is mixed with the circulating liquid in the first reboiler 9 and the second reboiler 10 through the system cold energy maintaining pipeline 4 and then enters the shell pass of the first main condenser 11 and the shell pass of the second main condenser 12 respectively to maintain the stability of the corresponding first rectifying tower 7 and the first rectifying tower 8 systems, so that the fluctuation of the systems is avoided to influence the purity of carbon monoxide; the circulating liquid returns to the heat pump 1 through the second circulating gas inlet 33, the second circulating gas outlet 34 of the heat exchanger 19 and the circulating inlet 5 of the heat pump 1 after passing through the shell side of the first main condenser 11 and the shell side of the second main condenser 12; the shell side outlet recycle gas temperature of the first main condenser 11 is: -177 to-181 ℃, gas phase fraction: 0.97, the shell side circulating gas temperature of the second main condenser 12 is: -178 to-182 ℃, gas phase fraction: 0.99, the temperature of the recycle gas after passing through the second recycle gas outlet 34 of the heat exchanger 19 is 35-40 ℃, and the gas phase fraction is as follows: 1.
according to the heat pump circulation system manufactured according to the scheme, the carbon monoxide production device and the production method with the heat pump circulation system, the first main condenser and the second main condenser are arranged, so that the defect of insufficient cold quantity at the top of the rectifying tower can be avoided, and the fluctuation of the product purity of carbon monoxide is caused; the nitrogen gas-liquid separation tank is arranged to enable nitrogen gas coming out of the heat pump to carry out gas-liquid separation, so that gas phase meets the heat load of a reboiler, meanwhile, circulating liquid at the outlet of the reboiler is mixed with liquid phase in the gas-liquid separation tank and then enters the first main condenser and the second main condenser to solve the problem of insufficient cold energy at the top of the rectifying tower, thereby achieving the purposes of stabilizing the rectifying system and ensuring the purity of products; the heat pump nitrogen circulation system is matched with the electronic carbon monoxide production device, so that the system can avoid fluctuation and further improve the purity of the product; the method has the characteristics of simple operation, stable operation, low power consumption of unit product and capability of improving the purity of the product to 99.9999% of electronic grade; provides a guarantee for the application development of the electronic grade carbon monoxide in the semiconductor field, and creates good economic and social benefits.
Drawings
Fig. 1 is a schematic structural view of the present invention.
FIG. 2 is a schematic diagram of a carbon monoxide production plant according to the present invention.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments.
Referring to fig. 1-2, a heat pump circulation system includes a heat pump 1, a circulation outlet 2 of the heat pump 1 is connected with an inlet of a nitrogen gas-liquid separation tank 3, a gas phase outlet at the top of the nitrogen gas-liquid separation tank 3 is respectively connected with reboilers at the lower parts in a plurality of rectifying towers, a liquid phase outlet at the bottom of the nitrogen gas-liquid separation tank 3 is respectively connected with shell passes of main condensers corresponding to the rectifying towers through a system cold energy maintaining pipeline 4, and a shell pass outlet of the main condensers is connected with a circulation inlet 5 of the heat pump 1.
Further, a first regulating valve 6 is respectively arranged between the reboiler at the lower part in the plurality of rectifying towers and the gas phase outlet of the nitrogen gas-liquid separation tank 3. And the outlets of reboilers at the lower parts in the rectifying towers are respectively communicated with a system cold maintaining pipeline 4.
Further, the rectifying tower comprises a first rectifying tower 7 and a second rectifying tower 8; the inner lower part of the first rectifying tower 7 is provided with a first reboiler 9, and the inner lower part of the second rectifying tower 8 is provided with a second reboiler 10; the first rectifying tower 7 is correspondingly provided with a first main condenser 11, and the second rectifying tower 8 is correspondingly provided with a second main condenser 12.
Further, a first tee joint 13 is arranged between the outlet of the reboiler and the system cold energy maintaining pipeline 4, a second tee joint 14 is arranged between the inlet of the shell side of the main condenser and the system cold energy maintaining pipeline 4, and a second regulating valve 15 is arranged on the system cold energy maintaining pipeline 4 between the first tee joint 13 and the second tee joint 14.
Further, a third regulating valve 16 is arranged between the shell side inlet of the main condenser and the second tee 13.
The invention also provides a production device of carbon monoxide, which comprises a raw material gas storage tank 17, a product tank 18, a first rectifying tower 7, a first reboiler 9, a first main condenser 11, a second rectifying tower 8, a second reboiler 10, a second main condenser 12 and the heat pump nitrogen circulation system.
Further, the feed gas storage tank 17 is connected with the feed gas inlet of the first rectifying tower 7 through the feed gas inlet 29 of the heat exchanger 19 and the feed gas outlet 30 of the heat exchanger 19, the liquid phase outlet at the bottom of the first rectifying tower 7 is connected with the first feed gas inlet 20 of the second rectifying tower 8 through the sixth regulating valve 27, the gas phase outlet at the top of the second rectifying tower 8 is connected with the liquid storage tank 22 through the tube pass of the second main condenser 12, and the liquid phase outlet at the bottom of the liquid storage tank 22 is respectively connected with the product tank 18 and the second feed gas inlet 21 at the middle upper part of the second rectifying tower 8; the gas phase outlet at the top of the liquid storage tank 22 is connected with the tube side of the second main condenser 12; the circulation outlet 2 of the heat pump 1 in the heat pump nitrogen circulation system is connected with the inlet of the nitrogen gas-liquid separation tank 3 through the first circulation gas inlet 31 of the heat exchanger 19 and the first circulation gas outlet 32 of the heat exchanger 19; the shell side outlet of the main condenser is connected to the circulation inlet 5 of the heat pump 1 via the second circulation gas inlet 33 of the heat exchanger 19 and the second circulation gas outlet 34 of the heat exchanger 19.
Further, a gas phase outlet at the top of the first rectifying tower 7 is connected with a gas-liquid separation tank 23 through a tube pass of the first main condenser 11, a liquid phase of the gas-liquid separation tank 23 is connected with a liquid inlet at the middle upper part of the first rectifying tower 7, and a gas phase of the gas-liquid separation tank 23 is connected with an exhaust furnace 25 through a first exhaust gas inlet 35 of the heat exchanger 19, a first exhaust gas outlet 36 of the heat exchanger 19 and a fourth regulating valve 24; the liquid phase outlet at the bottom of the second rectifying tower 8 is connected with the waste gas furnace 25 through a fifth regulating valve 26, a second tail gas inlet 37 of the heat exchanger 19 and a second tail gas outlet 38 of the heat exchanger 19.
Further, a sixth regulating valve 27 is arranged between the liquid phase outlet at the bottom of the first rectifying tower 7 and the first raw material liquid inlet 20 of the second rectifying tower 8; a seventh regulating valve 28 is arranged between the liquid phase outlet at the bottom of the liquid storage tank 22 and the second raw material liquid inlet 21 at the middle upper part of the second rectifying tower 8.
The invention also provides a production method of the carbon monoxide production device, which comprises the following steps:
step one: the raw material gas in the raw material gas storage tank 17 sequentially enters the first rectifying tower 7 through the raw material gas inlet 29 of the heat exchanger 19, the raw material gas outlet 30 of the heat exchanger 19 and the raw material inlet of the first rectifying tower 7; the raw material gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: the temperature and pressure are 40 ℃ and are as follows: 0.7MpaG, flow: 2200 Nm/h, a gas phase fraction of 1, carbon monoxide mole fraction: 35%; the feed gas temperature at the feed gas outlet 30 of the heat exchanger 19 is: -163 to-170 ℃ and gas phase fraction of 1;
Step two: the raw material gas entering the first rectifying tower 7 in the first step is subjected to primary rectifying purification, the gas phase after primary rectifying purification enters the gas-liquid separation tank 23 through an outlet at the top of the first rectifying tower 7 and a tube side of the first main condenser 13 to carry out gas-liquid separation, the liquid phase after gas-liquid separation enters the first rectifying tower 7 through the bottom of the gas-liquid separation tank 23 and a liquid inlet at the middle upper part of the first rectifying tower 7 to continue primary rectifying purification, a gas phase outlet of the gas-liquid separation tank 23 enters the waste gas furnace 25 through a first tail gas inlet 35 of the heat exchanger 19, a first tail gas outlet 36 of the heat exchanger 19 and a fourth regulating valve 24, and the gas phase temperature in the gas-liquid separation tank 23 is as follows: -172 to-178 ℃, carbon monoxide mole fraction: 25-30%, gas phase fraction: 1, a step of;
step three: the liquid phase after primary rectification and purification in the first step and the second step sequentially enters the second rectifying tower 8 through a liquid phase outlet at the bottom of the first rectifying tower 7 and a sixth regulating valve 27, secondary rectification and purification are carried out, a gas phase after secondary rectification and purification enters a liquid storage tank 22 through a gas phase outlet at the top of the second rectifying tower 8 and a tube pass of the second main condenser 12, one part of the liquid phase in the liquid storage tank 22 enters the second rectifying tower 8 through a second raw material liquid inlet 21 at the middle and upper part of the second rectifying tower 8, and the other part of the liquid phase enters a product tank 18; the liquid phase temperature of the bottom liquid phase outlet of the first rectifying tower 7 is: -165 to-170 ℃, and the purity of CO is: 69-75%; the product temperature in the product tank 18 is: 172 to 179 ℃ below zero, and the purity is not lower than 99.9999 percent;
Step four: the gas phase of the liquid storage tank 22 in the third step is communicated with the tube side of the second main condenser 12 and enters the tube side of the second main condenser 12 to be condensed;
step five: in the third step, the waste liquid purified by the second rectification column 8 sequentially enters the waste gas furnace 25 through a liquid phase outlet at the bottom of the second rectification column 8, a fifth regulating valve 26, a second tail gas inlet 37 of the heat exchanger 19 and a second tail gas outlet 38 of the heat exchanger 19, and the temperature of the waste liquid at the bottom of the second rectification column 8 is: -166 to-171 ℃, the purity of CO is: 25-30%, gas phase fraction: 0;
step six: the circulating gas in the heat pump 1 sequentially enters the nitrogen gas-liquid separation tank 3 through the circulating outlet 2, the first circulating gas inlet 31 of the heat exchanger 19 and the first circulating gas outlet 32 of the heat exchanger 19, the gas phase outlet of the nitrogen gas-liquid separation tank 3 respectively enters the corresponding first reboiler 9 and second reboiler 10 through two first regulating valves 6, and the components of the circulating gas are as follows: nitrogen, hydrogen, argon, nitrogen mole fraction: 99 percent; the first recycle gas outlet 32 of the heat exchanger 19 has a recycle gas temperature of: -162 to-168 ℃; the temperature of the circulating liquid at the outlet of the first reboiler 9 is as follows: -162 to-168 ℃, gas phase fraction: 0; the temperature of the circulating liquid at the outlet of the second reboiler 10 is: -163 to-170 ℃, gas phase fraction: 0;
Step seven: the liquid phase outlet of the nitrogen gas-liquid separation tank 3 in the step six is mixed with the circulating liquid in the first reboiler 9 and the second reboiler 10 through the system cold energy maintaining pipeline 4 and then enters the shell pass of the first main condenser 11 and the shell pass of the second main condenser 12 respectively to maintain the stability of the corresponding first rectifying tower 7 and the first rectifying tower 8 systems, so that the fluctuation of the systems is avoided to influence the purity of carbon monoxide; the circulating liquid returns to the heat pump 1 through the second circulating gas inlet 33, the second circulating gas outlet 34 of the heat exchanger 19 and the circulating inlet 5 of the heat pump 1 after passing through the shell side of the first main condenser 11 and the shell side of the second main condenser 12; the shell side outlet recycle gas temperature of the first main condenser 11 is: -177 to-181 ℃, gas phase fraction: 0.97, the shell side circulating gas temperature of the second main condenser 12 is: -178 to-182 ℃, gas phase fraction: 0.99, the temperature of the recycle gas after passing through the second recycle gas outlet 34 of the heat exchanger 19 is 35-40 ℃, and the gas phase fraction is as follows: 1.
the circulation outlet 2 of the heat pump 1 and the circulation inlet 5 of the heat pump 1 in the nitrogen circulation system of the heat pump can be respectively provided with heat exchange systems, the heat exchange systems can be mutually influenced or mutually independent, the heat exchange systems can directly take the form of a heat exchanger 19 when being combined with a production device of electronic grade carbon monoxide, and can exchange heat when being combined with other cryogenic systems, and the heat exchange effect can reach the above-mentioned step six and step seven; the purity of the liquid carbon monoxide in the invention can reach not lower than 99.9999%, the purity has no corresponding national standard in China, and the carbon monoxide is classified into seven grades according to the enterprise standard of China Industrial gas university and foreign company: industrial grade: 99.0% or more, chemical purity grade: 99.5% or more, high purity grade: 99.97% or more, CVD grade: 99.99%, ULSI + Stage: 99.995% or more, ultra-high purity grade: 99.997% or more, study grade: 99.998%; reference is made to: the third volume of the national institute of Industrial gases, 1904, page table II, 1.5.19, national gas company, bottled carbon monoxide quality specifications. The books are published by the university of the company, china industry gas industry Association. The invention has the advantage that the mole fraction of carbon monoxide can be calculated: 35% of raw gas is prepared into liquid carbon monoxide with purity not lower than 99.9999%, the production process is stable and reliable, the method has the characteristics of stable operation, reasonable flow design and low energy consumption, on one hand, the method realizes the cyclic utilization of cold and heat, fully recovers cold energy, solves the problem of high energy consumption in the traditional process, on the other hand, stabilizes the system process, sets a nitrogen gas-liquid separation tank, separates liquid nitrogen possibly generated after heat exchange, enables a regulating valve to regulate the circulation gas quantity more accurately, provides stable heat load for rectification, ensures the stability of the system, and remarkably improves the product quality.
The technical solutions of the embodiments of the present invention will be clearly and completely described in the following in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present invention without making any inventive effort, are intended to fall within the scope of the present invention.
Example 1
The heat pump circulation system comprises a heat pump 1, wherein a circulation outlet 2 of the heat pump 1 is connected with an inlet of a nitrogen gas-liquid separation tank 3, a gas phase outlet at the top of the nitrogen gas-liquid separation tank 3 is respectively connected with reboilers at the lower parts in a plurality of rectifying towers, a liquid phase outlet at the bottom of the nitrogen gas-liquid separation tank 3 is respectively connected with shell passes of main condensers corresponding to the rectifying towers through a system cold energy maintaining pipeline 4, and the shell pass outlet of the main condensers is connected with a circulation inlet 5 of the heat pump 1. And a first regulating valve 6 is respectively arranged between the reboiler at the lower part in the plurality of rectifying towers and the gas phase outlet of the nitrogen gas-liquid separation tank 3. And the outlets of reboilers at the lower parts in the rectifying towers are respectively communicated with a system cold maintaining pipeline 4. The rectifying tower comprises a first rectifying tower 7 and a second rectifying tower 8; the inner lower part of the first rectifying tower 7 is provided with a first reboiler 9, and the inner lower part of the second rectifying tower 8 is provided with a second reboiler 10; the first rectifying tower 7 is correspondingly provided with a first main condenser 11, and the second rectifying tower 8 is correspondingly provided with a second main condenser 12. A first tee joint 13 is arranged between the outlet of the reboiler and the system cold energy maintaining pipeline 4, a second tee joint 14 is arranged between the inlet of the shell side of the main condenser and the system cold energy maintaining pipeline 4, and a second regulating valve 15 is arranged on the system cold energy maintaining pipeline 4 between the first tee joint 13 and the second tee joint 14. A third regulating valve 16 is arranged between the shell side inlet of the main condenser and the second tee 13.
The invention also provides a production device of carbon monoxide, which comprises a raw material gas storage tank 17, a product tank 18, a first rectifying tower 7, a first reboiler 9, a first main condenser 11, a second rectifying tower 8, a second reboiler 10, a second main condenser 12 and the heat pump nitrogen circulation system. The raw material gas storage tank 17 is connected with the raw material inlet of the first rectifying tower 7 through the raw material gas inlet 29 of the heat exchanger 19 and the raw material gas outlet 30 of the heat exchanger 19, the liquid phase outlet at the bottom of the first rectifying tower 7 is connected with the first raw material liquid inlet 20 of the second rectifying tower 8 through the sixth regulating valve 27, the gas phase outlet at the top of the second rectifying tower 8 is connected with the liquid storage tank 22 through the tube pass of the second main condenser 12, and the liquid phase outlet at the bottom of the liquid storage tank 22 is respectively connected with the product tank 18 and the second raw material liquid inlet 21 at the middle upper part of the second rectifying tower 8; the gas phase outlet at the top of the liquid storage tank 22 is connected with the tube side of the second main condenser 12; the circulation outlet 2 of the heat pump 1 in the heat pump nitrogen circulation system is connected with the inlet of the nitrogen gas-liquid separation tank 3 through the first circulation gas inlet 31 of the heat exchanger 19 and the first circulation gas outlet 32 of the heat exchanger 19; the shell side outlet of the main condenser is connected to the circulation inlet 5 of the heat pump 1 via the second circulation gas inlet 33 of the heat exchanger 19 and the second circulation gas outlet 34 of the heat exchanger 19. The gas phase outlet at the top of the first rectifying tower 7 is connected with a gas-liquid separation tank 23 through the tube side of a first main condenser 11, the liquid phase of the gas-liquid separation tank 23 is connected with the liquid inlet at the middle upper part of the first rectifying tower 7, and the gas phase of the gas-liquid separation tank 23 is connected with an exhaust furnace 25 through a first exhaust inlet 35 of a heat exchanger 19, a first exhaust outlet 36 of the heat exchanger 19 and a fourth regulating valve 24; the liquid phase outlet at the bottom of the second rectifying tower 8 is connected with the waste gas furnace 25 through a fifth regulating valve 26, a second tail gas inlet 37 of the heat exchanger 19 and a second tail gas outlet 38 of the heat exchanger 19. A sixth regulating valve 27 is arranged between the liquid phase outlet at the bottom of the first rectifying tower 7 and the first raw material liquid inlet 20 of the second rectifying tower 8; a seventh regulating valve 28 is arranged between the liquid phase outlet at the bottom of the liquid storage tank 22 and the second raw material liquid inlet 21 at the middle upper part of the second rectifying tower 8.
The invention also provides a production method of the carbon monoxide production device, which comprises the following steps:
step one: the raw material gas in the raw material gas storage tank 17 sequentially enters the first rectifying tower 7 through the raw material gas inlet 29 of the heat exchanger 19, the raw material gas outlet 30 of the heat exchanger 19 and the raw material inlet of the first rectifying tower 7; the raw material gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: the temperature and pressure are 40 ℃ and are as follows: 0.7MpaG, flow: 2200 Nm/h, a gas phase fraction of 1, carbon monoxide mole fraction: 35%; the feed gas temperature at the feed gas outlet 30 of the heat exchanger 19 is: -163 ℃ and gas phase fraction of 1;
step two: the raw material gas entering the first rectifying tower 7 in the first step is subjected to primary rectifying purification, the gas phase after primary rectifying purification enters the gas-liquid separation tank 23 through an outlet at the top of the first rectifying tower 7 and a tube side of the first main condenser 13 to carry out gas-liquid separation, the liquid phase after gas-liquid separation enters the first rectifying tower 7 through the bottom of the gas-liquid separation tank 23 and a liquid inlet at the middle upper part of the first rectifying tower 7 to continue primary rectifying purification, a gas phase outlet of the gas-liquid separation tank 23 enters the waste gas furnace 25 through a first tail gas inlet 35 of the heat exchanger 19, a first tail gas outlet 36 of the heat exchanger 19 and a fourth regulating valve 24, and the gas phase temperature in the gas-liquid separation tank 23 is as follows: -172 ℃, carbon monoxide mole fraction: 25%, gas phase fraction: 1, a step of;
Step three: the liquid phase after primary rectification and purification in the first step and the second step sequentially enters the second rectifying tower 8 through a liquid phase outlet at the bottom of the first rectifying tower 7 and a sixth regulating valve 27, secondary rectification and purification are carried out, a gas phase after secondary rectification and purification enters a liquid storage tank 22 through a gas phase outlet at the top of the second rectifying tower 8 and a tube pass of the second main condenser 12, one part of the liquid phase in the liquid storage tank 22 enters the second rectifying tower 8 through a second raw material liquid inlet 21 at the middle and upper part of the second rectifying tower 8, and the other part of the liquid phase enters a product tank 18; the liquid phase temperature of the bottom liquid phase outlet of the first rectifying tower 7 is: -165 ℃, CO purity: 69%; the product temperature in the product tank 18 is: 172 ℃ below zero, the purity is 99.99991%;
step four: the gas phase of the liquid storage tank 22 in the third step is communicated with the tube side of the second main condenser 12 and enters the tube side of the second main condenser 12 to be condensed;
step five: in the third step, the waste liquid purified by the second rectification column 8 sequentially enters the waste gas furnace 25 through a liquid phase outlet at the bottom of the second rectification column 8, a fifth regulating valve 26, a second tail gas inlet 37 of the heat exchanger 19 and a second tail gas outlet 38 of the heat exchanger 19, and the temperature of the waste liquid at the bottom of the second rectification column 8 is: -166 ℃, CO purity is: 25%, gas phase fraction: 0;
Step six: the circulating gas in the heat pump 1 sequentially enters the nitrogen gas-liquid separation tank 3 through the circulating outlet 2, the first circulating gas inlet 31 of the heat exchanger 19 and the first circulating gas outlet 32 of the heat exchanger 19, the gas phase outlet of the nitrogen gas-liquid separation tank 3 respectively enters the corresponding first reboiler 9 and second reboiler 10 through two first regulating valves 6, and the components of the circulating gas are as follows: nitrogen, hydrogen, argon, nitrogen mole fraction: 99 percent; the first recycle gas outlet 32 of the heat exchanger 19 has a recycle gas temperature of: -162 ℃; the temperature of the circulating liquid at the outlet of the first reboiler 9 is as follows: -162 ℃, gas phase fraction: 0; the temperature of the circulating liquid at the outlet of the second reboiler 10 is: -163 ℃, gas phase fraction: 0;
step seven: the liquid phase outlet of the nitrogen gas-liquid separation tank 3 in the step six is mixed with the circulating liquid in the first reboiler 9 and the second reboiler 10 through the system cold energy maintaining pipeline 4 and then enters the shell pass of the first main condenser 11 and the shell pass of the second main condenser 12 respectively to maintain the stability of the corresponding first rectifying tower 7 and the first rectifying tower 8 systems, so that the fluctuation of the systems is avoided to influence the purity of carbon monoxide; the circulating liquid returns to the heat pump 1 through the second circulating gas inlet 33, the second circulating gas outlet 34 of the heat exchanger 19 and the circulating inlet 5 of the heat pump 1 after passing through the shell side of the first main condenser 11 and the shell side of the second main condenser 12; the shell side outlet recycle gas temperature of the first main condenser 11 is: -177 ℃, gas phase fraction: 0.97, the shell side circulating gas temperature of the second main condenser 12 is: -178 ℃, gas phase fraction: 0.99, the temperature of the recycle gas after passing through the second recycle gas outlet 34 of the heat exchanger 19 is 35 ℃, gas phase fraction: 1.
Example two
The heat pump circulation system comprises a heat pump 1, wherein a circulation outlet 2 of the heat pump 1 is connected with an inlet of a nitrogen gas-liquid separation tank 3, a gas phase outlet at the top of the nitrogen gas-liquid separation tank 3 is respectively connected with reboilers at the lower parts in a plurality of rectifying towers, a liquid phase outlet at the bottom of the nitrogen gas-liquid separation tank 3 is respectively connected with shell passes of main condensers corresponding to the rectifying towers through a system cold energy maintaining pipeline 4, and the shell pass outlet of the main condensers is connected with a circulation inlet 5 of the heat pump 1. And a first regulating valve 6 is respectively arranged between the reboiler at the lower part in the plurality of rectifying towers and the gas phase outlet of the nitrogen gas-liquid separation tank 3. And the outlets of reboilers at the lower parts in the rectifying towers are respectively communicated with a system cold maintaining pipeline 4. The rectifying tower comprises a first rectifying tower 7 and a second rectifying tower 8; the inner lower part of the first rectifying tower 7 is provided with a first reboiler 9, and the inner lower part of the second rectifying tower 8 is provided with a second reboiler 10; the first rectifying tower 7 is correspondingly provided with a first main condenser 11, and the second rectifying tower 8 is correspondingly provided with a second main condenser 12. A first tee joint 13 is arranged between the outlet of the reboiler and the system cold energy maintaining pipeline 4, a second tee joint 14 is arranged between the inlet of the shell side of the main condenser and the system cold energy maintaining pipeline 4, and a second regulating valve 15 is arranged on the system cold energy maintaining pipeline 4 between the first tee joint 13 and the second tee joint 14. A third regulating valve 16 is arranged between the shell side inlet of the main condenser and the second tee 13.
The invention also provides a production device of carbon monoxide, which comprises a raw material gas storage tank 17, a product tank 18, a first rectifying tower 7, a first reboiler 9, a first main condenser 11, a second rectifying tower 8, a second reboiler 10, a second main condenser 12 and the heat pump nitrogen circulation system. The raw material gas storage tank 17 is connected with the raw material inlet of the first rectifying tower 7 through the raw material gas inlet 29 of the heat exchanger 19 and the raw material gas outlet 30 of the heat exchanger 19, the liquid phase outlet at the bottom of the first rectifying tower 7 is connected with the first raw material liquid inlet 20 of the second rectifying tower 8 through the sixth regulating valve 27, the gas phase outlet at the top of the second rectifying tower 8 is connected with the liquid storage tank 22 through the tube pass of the second main condenser 12, and the liquid phase outlet at the bottom of the liquid storage tank 22 is respectively connected with the product tank 18 and the second raw material liquid inlet 21 at the middle upper part of the second rectifying tower 8; the gas phase outlet at the top of the liquid storage tank 22 is connected with the tube side of the second main condenser 12; the circulation outlet 2 of the heat pump 1 in the heat pump nitrogen circulation system is connected with the inlet of the nitrogen gas-liquid separation tank 3 through the first circulation gas inlet 31 of the heat exchanger 19 and the first circulation gas outlet 32 of the heat exchanger 19; the shell side outlet of the main condenser is connected to the circulation inlet 5 of the heat pump 1 via the second circulation gas inlet 33 of the heat exchanger 19 and the second circulation gas outlet 34 of the heat exchanger 19. The gas phase outlet at the top of the first rectifying tower 7 is connected with a gas-liquid separation tank 23 through the tube side of a first main condenser 11, the liquid phase of the gas-liquid separation tank 23 is connected with the liquid inlet at the middle upper part of the first rectifying tower 7, and the gas phase of the gas-liquid separation tank 23 is connected with an exhaust furnace 25 through a first exhaust inlet 35 of a heat exchanger 19, a first exhaust outlet 36 of the heat exchanger 19 and a fourth regulating valve 24; the liquid phase outlet at the bottom of the second rectifying tower 8 is connected with the waste gas furnace 25 through a fifth regulating valve 26, a second tail gas inlet 37 of the heat exchanger 19 and a second tail gas outlet 38 of the heat exchanger 19. A sixth regulating valve 27 is arranged between the liquid phase outlet at the bottom of the first rectifying tower 7 and the first raw material liquid inlet 20 of the second rectifying tower 8; a seventh regulating valve 28 is arranged between the liquid phase outlet at the bottom of the liquid storage tank 22 and the second raw material liquid inlet 21 at the middle upper part of the second rectifying tower 8.
The invention also provides a production method of the carbon monoxide production device, which comprises the following steps:
step one: the raw material gas in the raw material gas storage tank 17 sequentially enters the first rectifying tower 7 through the raw material gas inlet 29 of the heat exchanger 19, the raw material gas outlet 30 of the heat exchanger 19 and the raw material inlet of the first rectifying tower 7; the raw material gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: the temperature and pressure are 40 ℃ and are as follows: 0.7MpaG, flow: 2200 Nm/h, a gas phase fraction of 1, carbon monoxide mole fraction: 35%; the feed gas temperature at the feed gas outlet 30 of the heat exchanger 19 is: -170 ℃ and gas phase fraction of 1;
step two: the raw material gas entering the first rectifying tower 7 in the first step is subjected to primary rectifying purification, the gas phase after primary rectifying purification enters the gas-liquid separation tank 23 through an outlet at the top of the first rectifying tower 7 and a tube side of the first main condenser 13 to carry out gas-liquid separation, the liquid phase after gas-liquid separation enters the first rectifying tower 7 through the bottom of the gas-liquid separation tank 23 and a liquid inlet at the middle upper part of the first rectifying tower 7 to continue primary rectifying purification, a gas phase outlet of the gas-liquid separation tank 23 enters the waste gas furnace 25 through a first tail gas inlet 35 of the heat exchanger 19, a first tail gas outlet 36 of the heat exchanger 19 and a fourth regulating valve 24, and the gas phase temperature in the gas-liquid separation tank 23 is as follows: -178 ℃, carbon monoxide mole fraction: 30%, gas phase fraction: 1, a step of;
Step three: the liquid phase after primary rectification and purification in the first step and the second step sequentially enters the second rectifying tower 8 through a liquid phase outlet at the bottom of the first rectifying tower 7 and a sixth regulating valve 27, secondary rectification and purification are carried out, a gas phase after secondary rectification and purification enters a liquid storage tank 22 through a gas phase outlet at the top of the second rectifying tower 8 and a tube pass of the second main condenser 12, one part of the liquid phase in the liquid storage tank 22 enters the second rectifying tower 8 through a second raw material liquid inlet 21 at the middle and upper part of the second rectifying tower 8, and the other part of the liquid phase enters a product tank 18; the liquid phase temperature of the bottom liquid phase outlet of the first rectifying tower 7 is: -170 ℃, CO purity is: 75%; the product temperature in the product tank 18 is: -179 ℃, with a purity of 99.9999%;
step four: the gas phase of the liquid storage tank 22 in the third step is communicated with the tube side of the second main condenser 12 and enters the tube side of the second main condenser 12 to be condensed;
step five: in the third step, the waste liquid purified by the second rectification column 8 sequentially enters the waste gas furnace 25 through a liquid phase outlet at the bottom of the second rectification column 8, a fifth regulating valve 26, a second tail gas inlet 37 of the heat exchanger 19 and a second tail gas outlet 38 of the heat exchanger 19, and the temperature of the waste liquid at the bottom of the second rectification column 8 is: -171 ℃, CO purity: 30%, gas phase fraction: 0;
Step six: the circulating gas in the heat pump 1 sequentially enters the nitrogen gas-liquid separation tank 3 through the circulating outlet 2, the first circulating gas inlet 31 of the heat exchanger 19 and the first circulating gas outlet 32 of the heat exchanger 19, the gas phase outlet of the nitrogen gas-liquid separation tank 3 respectively enters the corresponding first reboiler 9 and second reboiler 10 through two first regulating valves 6, and the components of the circulating gas are as follows: nitrogen, hydrogen, argon, nitrogen mole fraction: 99 percent; the first recycle gas outlet 32 of the heat exchanger 19 has a recycle gas temperature of: -168 ℃; the temperature of the circulating liquid at the outlet of the first reboiler 9 is as follows: -168 ℃, gas phase fraction: 0; the temperature of the circulating liquid at the outlet of the second reboiler 10 is: -170 ℃, gas phase fraction: 0;
step seven: the liquid phase outlet of the nitrogen gas-liquid separation tank 3 in the step six is mixed with the circulating liquid in the first reboiler 9 and the second reboiler 10 through the system cold energy maintaining pipeline 4 and then enters the shell pass of the first main condenser 11 and the shell pass of the second main condenser 12 respectively to maintain the stability of the corresponding first rectifying tower 7 and the first rectifying tower 8 systems, so that the fluctuation of the systems is avoided to influence the purity of carbon monoxide; the circulating liquid returns to the heat pump 1 through the second circulating gas inlet 33, the second circulating gas outlet 34 of the heat exchanger 19 and the circulating inlet 5 of the heat pump 1 after passing through the shell side of the first main condenser 11 and the shell side of the second main condenser 12; the shell side outlet recycle gas temperature of the first main condenser 11 is: -181 ℃, gas phase fraction: 0.97, the shell side circulating gas temperature of the second main condenser 12 is: -182 ℃, gas phase fraction: 0.99, the temperature of the recycle gas after passing through the second recycle gas outlet 34 of the heat exchanger 19 is 40 ℃, gas phase fraction: 1.
Example III
The heat pump circulation system comprises a heat pump 1, wherein a circulation outlet 2 of the heat pump 1 is connected with an inlet of a nitrogen gas-liquid separation tank 3, a gas phase outlet at the top of the nitrogen gas-liquid separation tank 3 is respectively connected with reboilers at the lower parts in a plurality of rectifying towers, a liquid phase outlet at the bottom of the nitrogen gas-liquid separation tank 3 is respectively connected with shell passes of main condensers corresponding to the rectifying towers through a system cold energy maintaining pipeline 4, and the shell pass outlet of the main condensers is connected with a circulation inlet 5 of the heat pump 1. And a first regulating valve 6 is respectively arranged between the reboiler at the lower part in the plurality of rectifying towers and the gas phase outlet of the nitrogen gas-liquid separation tank 3. And the outlets of reboilers at the lower parts in the rectifying towers are respectively communicated with a system cold maintaining pipeline 4. The rectifying tower comprises a first rectifying tower 7 and a second rectifying tower 8; the inner lower part of the first rectifying tower 7 is provided with a first reboiler 9, and the inner lower part of the second rectifying tower 8 is provided with a second reboiler 10; the first rectifying tower 7 is correspondingly provided with a first main condenser 11, and the second rectifying tower 8 is correspondingly provided with a second main condenser 12. A first tee joint 13 is arranged between the outlet of the reboiler and the system cold energy maintaining pipeline 4, a second tee joint 14 is arranged between the inlet of the shell side of the main condenser and the system cold energy maintaining pipeline 4, and a second regulating valve 15 is arranged on the system cold energy maintaining pipeline 4 between the first tee joint 13 and the second tee joint 14. A third regulating valve 16 is arranged between the shell side inlet of the main condenser and the second tee 13.
The invention also provides a production device of carbon monoxide, which comprises a raw material gas storage tank 17, a product tank 18, a first rectifying tower 7, a first reboiler 9, a first main condenser 11, a second rectifying tower 8, a second reboiler 10, a second main condenser 12 and the heat pump nitrogen circulation system. The raw material gas storage tank 17 is connected with the raw material inlet of the first rectifying tower 7 through the raw material gas inlet 29 of the heat exchanger 19 and the raw material gas outlet 30 of the heat exchanger 19, the liquid phase outlet at the bottom of the first rectifying tower 7 is connected with the first raw material liquid inlet 20 of the second rectifying tower 8 through the sixth regulating valve 27, the gas phase outlet at the top of the second rectifying tower 8 is connected with the liquid storage tank 22 through the tube pass of the second main condenser 12, and the liquid phase outlet at the bottom of the liquid storage tank 22 is respectively connected with the product tank 18 and the second raw material liquid inlet 21 at the middle upper part of the second rectifying tower 8; the gas phase outlet at the top of the liquid storage tank 22 is connected with the tube side of the second main condenser 12; the circulation outlet 2 of the heat pump 1 in the heat pump nitrogen circulation system is connected with the inlet of the nitrogen gas-liquid separation tank 3 through the first circulation gas inlet 31 of the heat exchanger 19 and the first circulation gas outlet 32 of the heat exchanger 19; the shell side outlet of the main condenser is connected to the circulation inlet 5 of the heat pump 1 via the second circulation gas inlet 33 of the heat exchanger 19 and the second circulation gas outlet 34 of the heat exchanger 19. The gas phase outlet at the top of the first rectifying tower 7 is connected with a gas-liquid separation tank 23 through the tube side of a first main condenser 11, the liquid phase of the gas-liquid separation tank 23 is connected with the liquid inlet at the middle upper part of the first rectifying tower 7, and the gas phase of the gas-liquid separation tank 23 is connected with an exhaust furnace 25 through a first exhaust inlet 35 of a heat exchanger 19, a first exhaust outlet 36 of the heat exchanger 19 and a fourth regulating valve 24; the liquid phase outlet at the bottom of the second rectifying tower 8 is connected with the waste gas furnace 25 through a fifth regulating valve 26, a second tail gas inlet 37 of the heat exchanger 19 and a second tail gas outlet 38 of the heat exchanger 19. A sixth regulating valve 27 is arranged between the liquid phase outlet at the bottom of the first rectifying tower 7 and the first raw material liquid inlet 20 of the second rectifying tower 8; a seventh regulating valve 28 is arranged between the liquid phase outlet at the bottom of the liquid storage tank 22 and the second raw material liquid inlet 21 at the middle upper part of the second rectifying tower 8.
The invention also provides a production method of the carbon monoxide production device, which comprises the following steps:
step one: the raw material gas in the raw material gas storage tank 17 sequentially enters the first rectifying tower 7 through the raw material gas inlet 29 of the heat exchanger 19, the raw material gas outlet 30 of the heat exchanger 19 and the raw material inlet of the first rectifying tower 7; the raw material gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: the temperature and pressure are 40 ℃ and are as follows: 0.7MpaG, flow: 2200 Nm/h, a gas phase fraction of 1, carbon monoxide mole fraction: 35%; the feed gas temperature at the feed gas outlet 30 of the heat exchanger 19 is: 166.5℃with a gas phase fraction of 1;
step two: the raw material gas entering the first rectifying tower 7 in the first step is subjected to primary rectifying purification, the gas phase after primary rectifying purification enters the gas-liquid separation tank 23 through an outlet at the top of the first rectifying tower 7 and a tube side of the first main condenser 13 to carry out gas-liquid separation, the liquid phase after gas-liquid separation enters the first rectifying tower 7 through the bottom of the gas-liquid separation tank 23 and a liquid inlet at the middle upper part of the first rectifying tower 7 to continue primary rectifying purification, a gas phase outlet of the gas-liquid separation tank 23 enters the waste gas furnace 25 through a first tail gas inlet 35 of the heat exchanger 19, a first tail gas outlet 36 of the heat exchanger 19 and a fourth regulating valve 24, and the gas phase temperature in the gas-liquid separation tank 23 is as follows: -175 ℃, carbon monoxide mole fraction: 27.5%, gas phase fraction: 1, a step of;
Step three: the liquid phase after primary rectification and purification in the first step and the second step sequentially enters the second rectifying tower 8 through a liquid phase outlet at the bottom of the first rectifying tower 7 and a sixth regulating valve 27, secondary rectification and purification are carried out, a gas phase after secondary rectification and purification enters a liquid storage tank 22 through a gas phase outlet at the top of the second rectifying tower 8 and a tube pass of the second main condenser 12, one part of the liquid phase in the liquid storage tank 22 enters the second rectifying tower 8 through a second raw material liquid inlet 21 at the middle and upper part of the second rectifying tower 8, and the other part of the liquid phase enters a product tank 18; the liquid phase temperature of the bottom liquid phase outlet of the first rectifying tower 7 is: -167.5 ℃, CO purity is: 72%; the product temperature in the product tank 18 is: -175.5 ℃ and a purity of 99.99993%;
step four: the gas phase of the liquid storage tank 22 in the third step is communicated with the tube side of the second main condenser 12 and enters the tube side of the second main condenser 12 to be condensed;
step five: in the third step, the waste liquid purified by the second rectification column 8 sequentially enters the waste gas furnace 25 through a liquid phase outlet at the bottom of the second rectification column 8, a fifth regulating valve 26, a second tail gas inlet 37 of the heat exchanger 19 and a second tail gas outlet 38 of the heat exchanger 19, and the temperature of the waste liquid at the bottom of the second rectification column 8 is: -168.5 ℃, CO purity of: 27.5%, gas phase fraction: 0;
Step six: the circulating gas in the heat pump 1 sequentially enters the nitrogen gas-liquid separation tank 3 through the circulating outlet 2, the first circulating gas inlet 31 of the heat exchanger 19 and the first circulating gas outlet 32 of the heat exchanger 19, the gas phase outlet of the nitrogen gas-liquid separation tank 3 respectively enters the corresponding first reboiler 9 and second reboiler 10 through two first regulating valves 6, and the components of the circulating gas are as follows: nitrogen, hydrogen, argon, nitrogen mole fraction: 99 percent; the first recycle gas outlet 32 of the heat exchanger 19 has a recycle gas temperature of: -165 ℃; the temperature of the circulating liquid at the outlet of the first reboiler 9 is as follows: -165 ℃, gas phase fraction: 0; the temperature of the circulating liquid at the outlet of the second reboiler 10 is: -166.5 ℃, gas phase fraction: 0;
step seven: the liquid phase outlet of the nitrogen gas-liquid separation tank 3 in the step six is mixed with the circulating liquid in the first reboiler 9 and the second reboiler 10 through the system cold energy maintaining pipeline 4 and then enters the shell pass of the first main condenser 11 and the shell pass of the second main condenser 12 respectively to maintain the stability of the corresponding first rectifying tower 7 and the first rectifying tower 8 systems, so that the fluctuation of the systems is avoided to influence the purity of carbon monoxide; the circulating liquid returns to the heat pump 1 through the second circulating gas inlet 33, the second circulating gas outlet 34 of the heat exchanger 19 and the circulating inlet 5 of the heat pump 1 after passing through the shell side of the first main condenser 11 and the shell side of the second main condenser 12; the shell side outlet recycle gas temperature of the first main condenser 11 is: -179 ℃, gas phase fraction: 0.97, the shell side circulating gas temperature of the second main condenser 12 is: -180 ℃, gas phase fraction: 0.99, the temperature of the recycle gas after passing through the second recycle gas outlet 34 of the heat exchanger 19 is 37.5 ℃, gas phase fraction: 1.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.

Claims (8)

1. A process for the production of carbon monoxide, the process comprising the steps of:
step one: the raw material gas in the raw material gas storage tank (17) sequentially enters the first rectifying tower (7) through the raw material gas inlet (29) of the heat exchanger (19), the raw material gas outlet (30) of the heat exchanger (19) and the raw material inlet of the first rectifying tower (7); the raw material gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: the temperature and pressure are 40 ℃ and are as follows: 0.7MpaG, flow: 2200 Nm/h, a gas phase fraction of 1, carbon monoxide mole fraction: 35%; the feed gas temperature at the feed gas outlet (30) of the heat exchanger (19) is: -163 to-170 ℃ and gas phase fraction of 1;
step two: the method comprises the steps that raw material gas entering a first rectifying tower (7) in the first step is subjected to primary rectifying purification, gas phase after primary rectifying purification enters a gas-liquid separation tank (23) through an outlet at the top of the first rectifying tower (7) and a tube side of a first main condenser (11) to be subjected to gas-liquid separation, liquid phase after gas-liquid separation enters the first rectifying tower (7) through the bottom of the gas-liquid separation tank (23) and a liquid inlet at the middle upper part of the first rectifying tower (7) to be subjected to primary rectifying purification, and a gas phase outlet of the gas-liquid separation tank (23) enters a waste gas furnace (25) through a first tail gas inlet (35) of a heat exchanger (19), a first tail gas outlet (36) of the heat exchanger (19) and a fourth regulating valve (24), wherein the gas phase temperature in the gas-liquid separation tank (23) is as follows: -172 to-178 ℃, carbon monoxide mole fraction: 25-30%, gas phase fraction: 1, a step of;
Step three: the liquid phase after primary rectification and purification in the first step and the second step sequentially enters the second rectifying tower (8) through a liquid phase outlet at the bottom of the first rectifying tower (7) and a sixth regulating valve (27), secondary rectification and purification are carried out, a gas phase after secondary rectification and purification enters a liquid storage tank (22) through a gas phase outlet at the top of the second rectifying tower (8) and a tube pass of the second main condenser (12), one part of the liquid phase in the liquid storage tank (22) enters the second rectifying tower (8) through a second raw material liquid inlet (21) at the upper part of the second rectifying tower (8), and the other part of the liquid phase enters a product tank (18); the liquid phase temperature of the bottom liquid phase outlet of the first rectifying tower (7) is as follows: -165 to-170 ℃, and the purity of CO is: 69-75%; the product temperature in the product tank (18) is: 172 to 179 ℃ below zero, and the purity is not lower than 99.9999 percent;
step four: the gas phase of the liquid storage tank (22) in the third step is communicated with the tube side of the second main condenser (12) and enters the tube side of the second main condenser (12) for condensation;
step five: in the third step, the waste liquid purified by the second rectification tower (8) sequentially enters the waste gas furnace (25) through a liquid phase outlet at the bottom of the second rectification tower (8), a fifth regulating valve (26), a second tail gas inlet (37) of the heat exchanger (19) and a second tail gas outlet (38) of the heat exchanger (19), and the temperature of the waste liquid at the bottom of the second rectification tower (8) is as follows: -166 to-171 ℃, the purity of CO is: 25-30%, gas phase fraction: 0;
Step six: circulating gas in the heat pump (1) sequentially passes through a circulating outlet (2), a first circulating gas inlet (31) of the heat exchanger (19) and a first circulating gas outlet (32) of the heat exchanger (19) to enter the nitrogen gas-liquid separation tank (3), and gas phase outlets of the nitrogen gas-liquid separation tank (3) respectively enter a first reboiler (9) and a second reboiler (10) which are respectively corresponding to each other through two first regulating valves (6), wherein the components of the circulating gas are as follows: nitrogen, hydrogen, argon, nitrogen mole fraction: 99 percent; the first recycle gas outlet (32) of the heat exchanger (19) has a recycle gas temperature of: -162 to-168 ℃; the temperature of the circulating liquid at the outlet of the first reboiler (9) is as follows: -162 to-168 ℃, gas phase fraction: 0; the temperature of the circulating liquid at the outlet of the second reboiler (10) is as follows: -163 to-170 ℃, gas phase fraction: 0;
step seven: the liquid phase outlet of the nitrogen gas-liquid separation tank (3) in the step six is mixed with circulating liquid in the first reboiler (9) and the second reboiler (10) through a system cold energy maintaining pipeline (4) and then enters the shell pass of the first main condenser (11) and the shell pass of the second main condenser (12) respectively; the circulating liquid returns to the heat pump (1) through the second circulating gas inlet (33), the second circulating gas outlet (34) of the heat exchanger (19) and the circulating inlet (5) of the heat pump (1) after passing through the shell side of the first main condenser (11) and the shell side of the second main condenser (12); the shell side outlet recycle gas temperature of the first main condenser (11) is as follows: -177 to-181 ℃, gas phase fraction: 0.97, the shell side circulating gas temperature of the second main condenser (12) is: -178 to-182 ℃, gas phase fraction: 0.99, the temperature of the circulating gas after passing through the second circulating gas outlet (34) of the heat exchanger (19) is 35-40 ℃, and the gas phase fraction is as follows: 1.
2. A process for the production of carbon monoxide as claimed in claim 1, wherein: the system comprises a raw material gas storage tank (17), a product tank (18), a first rectifying tower (7), a first reboiler (9), a first main condenser (11), a second rectifying tower (8), a second reboiler (10), a second main condenser (12) and a heat pump circulation system;
the heat pump circulation system comprises a heat pump (1), a circulation outlet (2) of the heat pump (1) is connected with an inlet of a nitrogen gas-liquid separation tank (3), a gas phase outlet at the top of the nitrogen gas-liquid separation tank (3) is respectively connected with reboilers at the inner lower parts of a plurality of rectifying towers, a liquid phase outlet at the bottom of the nitrogen gas-liquid separation tank (3) is respectively connected with shell passes of main condensers corresponding to the two rectifying towers through a system cold energy maintaining pipeline (4), and a shell pass outlet of the main condenser is connected with a circulation inlet (5) of the heat pump (1).
3. A method for producing carbon monoxide according to claim 2, wherein: the rectifying tower comprises a first rectifying tower (7) and a second rectifying tower (8);
the inner lower part of the first rectifying tower (7) is provided with a first reboiler (9), and the inner lower part of the second rectifying tower (8) is provided with a second reboiler (10);
The first rectifying tower (7) is correspondingly provided with a first main condenser (11), and the second rectifying tower (8) is correspondingly provided with a second main condenser (12).
4. A method for producing carbon monoxide according to claim 2, wherein: a first tee joint (13) is arranged between the outlet of the reboiler and the system cold energy maintaining pipeline (4), a second tee joint (14) is arranged between the shell side inlet of the main condenser and the system cold energy maintaining pipeline (4), and a second regulating valve (15) is arranged on the system cold energy maintaining pipeline (4) between the first tee joint (13) and the second tee joint (14).
5. The method for producing carbon monoxide according to claim 4, wherein: a third regulating valve (16) is arranged between the shell side inlet of the main condenser and the second tee joint (14).
6. A method for producing carbon monoxide according to claim 2, wherein: the feed gas storage tank (17) is connected with the feed gas inlet of the first rectifying tower (7) through the feed gas inlet (29) of the heat exchanger (19) and the feed gas outlet (30) of the heat exchanger (19), the liquid phase outlet at the bottom of the first rectifying tower (7) is connected with the first feed liquid inlet (20) of the second rectifying tower (8), the gas phase outlet at the top of the second rectifying tower (8) is connected with the liquid storage tank (22) through the tube pass of the second main condenser (12), and the liquid phase outlet at the bottom of the liquid storage tank (22) is respectively connected with the product tank (18) and the second feed liquid inlet (21) at the upper part of the second rectifying tower (8); the gas phase outlet at the top of the liquid storage tank (22) is connected with the tube side of the second main condenser (12);
A circulation outlet (2) of a heat pump (1) in the heat pump nitrogen circulation system is connected with an inlet of a nitrogen gas-liquid separation tank (3) through a first circulation gas inlet (31) of a heat exchanger (19) and a first circulation gas outlet (32) of the heat exchanger (19);
the shell side outlet of the main condenser is connected with the circulating inlet (5) of the heat pump (1) through the second circulating gas inlet (33) of the heat exchanger (19) and the second circulating gas outlet (34) of the heat exchanger (19).
7. The method for producing carbon monoxide according to claim 6, wherein: the outlet at the top of the first rectifying tower (7) is connected with a gas-liquid separation tank (23) through a tube pass of a first main condenser (11), the liquid phase of the gas-liquid separation tank (23) is connected with a liquid inlet at the middle upper part of the first rectifying tower (7), and the gas phase of the gas-liquid separation tank (23) is connected with an exhaust furnace (25) through a first exhaust inlet (35) of a heat exchanger (19), a first exhaust outlet (36) of the heat exchanger (19) and a fourth regulating valve (24);
the liquid phase outlet at the bottom of the second rectifying tower (8) is connected with the waste gas furnace (25) through a fifth regulating valve (26), a second tail gas inlet (37) of the heat exchanger (19) and a second tail gas outlet (38) of the heat exchanger (19).
8. The method for producing carbon monoxide according to claim 6, wherein: a sixth regulating valve (27) is arranged between the liquid phase outlet at the bottom of the first rectifying tower (7) and the first raw material liquid inlet (20) of the second rectifying tower (8);
a seventh regulating valve (28) is arranged between the liquid phase outlet at the bottom of the liquid storage tank (22) and the second raw material liquid inlet (21) at the upper middle part of the second rectifying tower (8).
CN202010153513.1A 2020-03-06 2020-03-06 Heat pump circulation system, carbon monoxide production device with heat pump circulation system and carbon monoxide production method Active CN111141109B (en)

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CN106288651A (en) * 2016-08-29 2017-01-04 河南心连心深冷能源股份有限公司 Device and the production method of ultra-pure carbon monoxide is produced with nitrogen heat pump rectification
CN208042614U (en) * 2018-02-06 2018-11-02 河南心连心深冷能源股份有限公司 A kind of ice chest that can produce technical grade and high-purity carbon monooxide
CN110057164A (en) * 2019-03-20 2019-07-26 河南心连心深冷能源股份有限公司 It is a kind of to produce water content≤30ppb electron level CO2Device and production method
CN110553464A (en) * 2019-08-29 2019-12-10 杭州中泰深冷技术股份有限公司 CO cryogenic separation system and method for reducing nitrogen circulation energy consumption
CN211716982U (en) * 2020-03-06 2020-10-20 河南心连心深冷能源股份有限公司 Heat pump circulation system and carbon monoxide production device with same

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106288651A (en) * 2016-08-29 2017-01-04 河南心连心深冷能源股份有限公司 Device and the production method of ultra-pure carbon monoxide is produced with nitrogen heat pump rectification
CN208042614U (en) * 2018-02-06 2018-11-02 河南心连心深冷能源股份有限公司 A kind of ice chest that can produce technical grade and high-purity carbon monooxide
CN110057164A (en) * 2019-03-20 2019-07-26 河南心连心深冷能源股份有限公司 It is a kind of to produce water content≤30ppb electron level CO2Device and production method
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