CN111141109A - Heat pump circulating system, carbon monoxide production device with heat pump circulating system and carbon monoxide production method - Google Patents

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

Info

Publication number
CN111141109A
CN111141109A CN202010153513.1A CN202010153513A CN111141109A CN 111141109 A CN111141109 A CN 111141109A CN 202010153513 A CN202010153513 A CN 202010153513A CN 111141109 A CN111141109 A CN 111141109A
Authority
CN
China
Prior art keywords
gas
outlet
liquid
rectifying tower
inlet
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.)
Granted
Application number
CN202010153513.1A
Other languages
Chinese (zh)
Other versions
CN111141109B (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
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Henan Xinlianxin Shenleng Energy Co ltd
Original Assignee
Henan Xinlianxin Shenleng Energy Co ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Henan Xinlianxin Shenleng Energy Co ltd filed Critical Henan Xinlianxin Shenleng Energy Co ltd
Priority to CN202010153513.1A priority Critical patent/CN111141109B/en
Publication of CN111141109A publication Critical patent/CN111141109A/en
Application granted granted Critical
Publication of CN111141109B publication Critical patent/CN111141109B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

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
    • F25J3/0204—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
    • 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
    • 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

Landscapes

  • 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 circulating system, a carbon monoxide production device with the heat pump circulating system and a carbon monoxide production method with the heat pump circulating 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 lower parts in 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 which respectively correspond to the plurality of rectifying towers through a system cold energy maintaining pipeline, and the shell pass outlet of the main condenser is connected with the circulating inlet of the heat pump; has the characteristics of simple and convenient operation, stable operation, low power consumption of unit product and capability of improving the product purity to 99.9999 percent of electronic grade.

Description

Heat pump circulating system, carbon monoxide production device with heat pump circulating 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 circulation system, a carbon monoxide production device with the heat pump circulation system and a carbon monoxide production method with the heat pump circulation system.
Background
In the existing production method of carbon monoxide, the processes of PSA-CO, heat pump rectification and the like are mainly adopted. The existing PSA-CO process by pressure swing adsorption has the following defects: the system occupies large area, the equipment investment is large, the flow is complex and the product purity is not high; the heat pump rectification process has the characteristics of less equipment investment, small occupied area and high product purity and is widely applied, but the existing heat pump rectification process has the defects of insufficient tower top cold quantity of a rectification tower, unstable system operation and fluctuation of product purity; 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 a heat pump circulating system which has the advantages of simple structure, reasonable design, more stable operation of a heat pump rectification process system, capability of further producing high-purity carbon monoxide, low energy consumption and cyclic utilization, and a carbon monoxide production device and a carbon monoxide production method with the heat pump circulating system.
In order to achieve the purpose, the invention provides the following technical scheme: the utility model provides a heat pump circulation system, this circulation system includes the heat pump, and the circulation outlet of heat pump links to each other with the import of nitrogen gas-liquid separation jar, and the gaseous phase export at nitrogen gas-liquid separation jar top links to each other with the reboiler of lower part in a plurality of rectifying column respectively, and the liquid phase export of nitrogen gas-liquid separation jar bottom is maintained the pipeline through system's cold volume and is linked to each other with the shell side of the respective corresponding main condenser of a plurality of rectifying column respectively, and the shell side export of main condenser links to each other with the circulation import of 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 tank; and the outlets of the reboilers at the lower parts in the plurality of rectifying towers are respectively communicated with a system cold energy maintaining pipeline.
Preferably, the rectifying tower comprises a first rectifying tower and a second rectifying tower; a first reboiler is arranged at the inner lower part of the first rectifying tower, and a second reboiler is arranged at the inner lower part of the second rectifying tower; 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 feed 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 a raw material inlet of the first rectifying tower through a raw material gas inlet of the heat exchanger and a raw material gas outlet of the heat exchanger, a liquid phase outlet at the bottom of the first rectifying tower is connected with a first raw material liquid inlet of the second rectifying tower, a gas phase outlet at the top of the second rectifying tower is connected with the liquid storage tank through a tube pass of the second main condenser, and a liquid phase outlet at the bottom of the liquid storage tank is respectively connected with the product tank and a second raw material liquid inlet at the middle upper part of the second rectifying tower; a gas phase outlet at the top of the liquid storage tank is connected with a tube pass of the second main condenser; a circulating outlet of a heat pump in the heat pump nitrogen circulating system is connected with an inlet of the nitrogen gas-liquid separation tank through a first circulating gas inlet of the heat exchanger and a first circulating gas outlet of the heat exchanger; and the shell side outlet of the main condenser is connected with the circulating inlet of the heat pump through a second circulating gas inlet of the heat exchanger and a second circulating gas outlet of the heat exchanger.
Preferably, an outlet at the top of the first rectifying tower is connected with a gas-liquid separation tank through a tube side of a first main condenser, a liquid phase of the gas-liquid separation tank is connected with a liquid inlet at the middle upper part of the first rectifying tower, and a gas phase of the gas-liquid separation tank is connected with the waste gas furnace through a first tail gas inlet of the heat exchanger, a first tail gas outlet of the heat exchanger and a fourth regulating valve; and a 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 middle upper part of the second rectifying tower.
The invention also provides a production method of the carbon monoxide production device, which comprises the following steps:
the method comprises the following steps: the raw material gas in the raw material gas storage tank 17 sequentially passes through a raw material gas inlet 29 of the heat exchanger 19, a raw material gas outlet 30 of the heat exchanger 19 and a raw material inlet of the first rectifying tower 7 to enter the first rectifying tower 7; the feed gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: at 40 ℃ and under a pressure of: 0.7MpaG, flow: 2200 Nm/h, fraction in gas phase 1, molar fraction of carbon monoxide: 35 percent; the feed gas temperature at feed gas outlet 30 of heat exchanger 19 is: the gas phase fraction is 1 at-163 to-170 ℃;
step two: the raw material gas entering the first rectifying tower 7 in the first step is subjected to primary rectification and purification, the gas phase after primary rectification and purification enters the gas-liquid separation tank 23 through an outlet at the top of the first rectifying tower 7 and a tube pass of the first main condenser 13 to be subjected to 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 be subjected to primary rectification and purification continuously, the gas phase outlet of the gas-liquid separation tank 23 enters the waste gas furnace 25 through the first tail gas inlet 35 of the heat exchanger 19, the first tail gas outlet 36 of the heat exchanger 19 and the fourth regulating valve 24, and the gas phase temperature in the gas-liquid separation tank 23 is as follows: -172 to-178 ℃, carbon monoxide molar fraction: 25-30%, gas phase fraction: 1;
step three: the liquid phase purified by the primary rectification in the first step and the second step sequentially passes through a liquid phase outlet at the bottom of the first rectifying tower 7 and a sixth regulating valve 27 to enter the second rectifying tower 8 for secondary rectification and purification, the gas phase purified by the secondary rectification enters the 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 upper part of the second rectifying tower 8, and the other part of the liquid phase enters the product tank 18; the liquid phase temperature at the bottom liquid phase outlet of the first rectifying tower 7 is as follows: -165 to-170 ℃, CO purity: 69-75%; the product temperature in the product tank 18 is: the purity is not lower than 99.9999 percent at the temperature of-172 to-179 ℃;
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 after the secondary rectification and purification through the second rectification tower 8 sequentially passes through the liquid phase outlet at the bottom of the second rectification tower 8, the fifth regulating valve 26, the second tail gas inlet 37 of the heat exchanger 19 and the second tail gas outlet 38 of the heat exchanger 19 to enter the waste gas furnace 25, and the temperature of the waste liquid at the bottom of the second rectification tower 8 is as follows: -166 to-171 ℃, and the CO purity 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 a heat exchanger 19 and a first circulating gas outlet 32 of the heat exchanger 19 to enter a nitrogen gas-liquid separation tank 3, a gas phase outlet of the nitrogen gas-liquid separation tank 3 respectively enters a first reboiler 9 and a second reboiler 10 which respectively correspond to the first reboiler 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 cycle gas temperature at the first cycle gas outlet 32 of the heat exchanger 19 is: -162 to-168 ℃; the temperature of the circulating liquid at the outlet of the first reboiler 9 was: -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 sixth step 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 respectively enters the shell pass of the first main condenser 11 and the shell pass of the second main condenser 12 to be used for maintaining the stability of the corresponding first rectifying tower 7 and the first rectifying tower 8 system, so that the influence on the purity of carbon monoxide caused by the fluctuation of the system is avoided; the circulating liquid passes through the shell side of the first main condenser 11 and the shell side of the second main condenser 12 and then returns to the heat pump 1 through a second circulating gas inlet 33, a second circulating gas outlet 34 of the heat exchanger 19 and a circulating inlet 5 of the heat pump 1; the shell-side outlet circulating gas temperature of the first main condenser 11 is as follows: -177 to-181 ℃, gas phase fraction: 0.97, the shell-side recycle gas temperature of the second main condenser 12 is: -178 to-182 ℃, gas phase fraction: 0.99, the temperature of the circulating gas passing through a second circulating gas outlet 34 of the heat exchanger 19 is 35-40 ℃, and the gas phase fraction: 1.
according to the heat pump circulating system manufactured according to the scheme, the carbon monoxide production device with the heat pump circulating system and the carbon monoxide production method with the heat pump circulating system, the first main condenser and the second main condenser are arranged, so that the problem that the product purity of carbon monoxide fluctuates due to insufficient cold energy at the top of the rectifying tower can be avoided; the nitrogen gas from the heat pump can be subjected to gas-liquid separation by arranging the nitrogen gas-liquid separation tank, so that a 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 cooling capacity at the top of the rectifying tower, so that the aims of stabilizing the rectifying system and ensuring the purity of a product are fulfilled, meanwhile, the circulating gas can be circulated in the system by arranging the heat pump, and further, the aim of recovering the energy of the circulating gas is fulfilled by arranging the heat exchanger; the nitrogen circulating system of the heat pump is matched with the production device of the electronic grade carbon monoxide, so that the system can avoid fluctuation, and the product purity is further improved; the method has the characteristics of simple and convenient operation, stable operation, low power consumption of unit products and capability of improving the product purity to 99.9999 percent of electronic grade; the method provides guarantee for the application and development of electronic-grade carbon monoxide in the field of semiconductors, and creates good economic and social benefits.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
FIG. 2 is a schematic structural diagram of a carbon monoxide production apparatus according to the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
Referring to fig. 1-2, a heat pump cycle system includes a heat pump 1, a cycle 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 part 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 plurality of rectifying towers through a system cold energy maintaining pipeline 4, and a shell pass outlet of the main condenser is connected with a cycle inlet 5 of the heat pump 1.
Further, a first adjusting valve 6 is respectively arranged between a reboiler at the lower part in the plurality of rectifying towers and a gas phase outlet of the nitrogen gas-liquid separation tank 3. The outlets of the reboilers at the lower part in the plurality of rectifying towers are respectively communicated with a system cold energy maintaining pipeline 4.
Further, the rectifying tower comprises a first rectifying tower 7 and a second rectifying tower 8; a first reboiler 9 is arranged at the inner lower part of the first rectifying tower 7, and a second reboiler 10 is arranged at the inner lower part of the second rectifying tower 8; 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.
Furthermore, 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.
Further, a third regulating valve 16 is arranged between the shell side inlet of the main condenser and the second tee joint 13.
The invention also provides a carbon monoxide production device, 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 raw material gas storage tank 17 is connected with a raw material inlet of the first rectifying tower 7 through a raw material gas inlet 29 of the heat exchanger 19 and a raw material gas outlet 30 of the heat exchanger 19, a liquid phase outlet at the bottom of the first rectifying tower 7 is connected with a first raw material liquid inlet 20 of the second rectifying tower 8 through a sixth regulating valve 27, a gas phase outlet at the top of the second rectifying tower 8 is connected with the liquid storage tank 22 through a tube pass of the second main condenser 12, and a liquid phase outlet at the bottom of the liquid storage tank 22 is respectively connected with the product tank 18 and a second raw material liquid inlet 21 at the upper middle part of the second rectifying tower 8; a 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 circulation inlet 5 of the heat pump 1 through a second circulation gas inlet 33 of the heat exchanger 19 and a 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 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 a 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:
the method comprises the following steps: the raw material gas in the raw material gas storage tank 17 sequentially passes through a raw material gas inlet 29 of the heat exchanger 19, a raw material gas outlet 30 of the heat exchanger 19 and a raw material inlet of the first rectifying tower 7 to enter the first rectifying tower 7; the feed gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: at 40 ℃ and under a pressure of: 0.7MpaG, flow: 2200 Nm/h, fraction in gas phase 1, molar fraction of carbon monoxide: 35 percent; the feed gas temperature at feed gas outlet 30 of heat exchanger 19 is: the gas phase fraction is 1 at-163 to-170 ℃;
step two: the raw material gas entering the first rectifying tower 7 in the first step is subjected to primary rectification and purification, the gas phase after primary rectification and purification enters the gas-liquid separation tank 23 through an outlet at the top of the first rectifying tower 7 and a tube pass of the first main condenser 13 to be subjected to 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 be subjected to primary rectification and purification continuously, the gas phase outlet of the gas-liquid separation tank 23 enters the waste gas furnace 25 through the first tail gas inlet 35 of the heat exchanger 19, the first tail gas outlet 36 of the heat exchanger 19 and the fourth regulating valve 24, and the gas phase temperature in the gas-liquid separation tank 23 is as follows: -172 to-178 ℃, carbon monoxide molar fraction: 25-30%, gas phase fraction: 1;
step three: the liquid phase purified by the primary rectification in the first step and the second step sequentially passes through a liquid phase outlet at the bottom of the first rectifying tower 7 and a sixth regulating valve 27 to enter the second rectifying tower 8 for secondary rectification and purification, the gas phase purified by the secondary rectification enters the 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 upper part of the second rectifying tower 8, and the other part of the liquid phase enters the product tank 18; the liquid phase temperature at the bottom liquid phase outlet of the first rectifying tower 7 is as follows: -165 to-170 ℃, CO purity: 69-75%; the product temperature in the product tank 18 is: the purity is not lower than 99.9999 percent at the temperature of-172 to-179 ℃;
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 after the secondary rectification and purification through the second rectification tower 8 sequentially passes through the liquid phase outlet at the bottom of the second rectification tower 8, the fifth regulating valve 26, the second tail gas inlet 37 of the heat exchanger 19 and the second tail gas outlet 38 of the heat exchanger 19 to enter the waste gas furnace 25, and the temperature of the waste liquid at the bottom of the second rectification tower 8 is as follows: -166 to-171 ℃, and the CO purity 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 a heat exchanger 19 and a first circulating gas outlet 32 of the heat exchanger 19 to enter a nitrogen gas-liquid separation tank 3, a gas phase outlet of the nitrogen gas-liquid separation tank 3 respectively enters a first reboiler 9 and a second reboiler 10 which respectively correspond to the first reboiler 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 cycle gas temperature at the first cycle gas outlet 32 of the heat exchanger 19 is: -162 to-168 ℃; the temperature of the circulating liquid at the outlet of the first reboiler 9 was: -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 sixth step 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 respectively enters the shell pass of the first main condenser 11 and the shell pass of the second main condenser 12 to be used for maintaining the stability of the corresponding first rectifying tower 7 and the first rectifying tower 8 system, so that the influence on the purity of carbon monoxide caused by the fluctuation of the system is avoided; the circulating liquid passes through the shell side of the first main condenser 11 and the shell side of the second main condenser 12 and then returns to the heat pump 1 through a second circulating gas inlet 33, a second circulating gas outlet 34 of the heat exchanger 19 and a circulating inlet 5 of the heat pump 1; the shell-side outlet circulating gas temperature of the first main condenser 11 is as follows: -177 to-181 ℃, gas phase fraction: 0.97, the shell-side recycle gas temperature of the second main condenser 12 is: -178 to-182 ℃, gas phase fraction: 0.99, the temperature of the circulating gas passing through a second circulating gas outlet 34 of the heat exchanger 19 is 35-40 ℃, and the gas phase fraction: 1.
the heat pump nitrogen circulating system of the invention has the advantages that the circulating outlet 2 of the heat pump 1 and the circulating inlet 5 of the heat pump 1 can be respectively provided with a heat exchange system, the heat exchange systems can be mutually influenced or mutually independent, when the heat pump nitrogen circulating system is combined with an electronic grade carbon monoxide production device, the heat exchanger 19 can be directly adopted, when the heat pump nitrogen circulating system is combined with other cryogenic systems, the heat exchange can be carried out by combining with other systems, and the heat exchange effect can reach the sixth step and the seventh step; the purity of the liquid carbon monoxide in the invention can reach not less than 99.9999 percent, the purity has no corresponding national standard in China, and the carbon monoxide is divided into seven grades according to the Chinese Industrial gas complete and the enterprise standard of foreign companies: industrial grade: not less than 99.0%, chemical purity grade: not less than 99.5%, high purity grade: not less than 99.97%, CVD grade: 99.99%, ULSI+Stage (2): not less than 99.995%, ultra-high purity grade: not less than 99.997%, research grade: 99.998 percent; reference documents: the third book of the national Industrial gas university, 1904 page table II, 1.5.19 foreign gas company bottled technical indicators for the amount of carbon monoxide. The book was published by the university press of the university, authored by the gas industry association of china. The invention has the advantages that the molar fraction of carbon monoxide can be adjusted as follows:the method is characterized in that 35% of raw gas is prepared into liquid carbon monoxide with the purity not lower than 99.9999%, the production process is stable and reliable, and the method has the characteristics of stable operation, reasonable flow design and low energy consumption.
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without any inventive step, are within the scope of the present invention.
Example one
The utility model provides a heat pump circulation system, includes heat pump 1, and the circulation export 2 of heat pump 1 links to each other with nitrogen gas-liquid separation jar 3 import, and the gaseous phase export at 3 tops of nitrogen gas-liquid separation jar links to each other with the reboiler of lower part in a plurality of rectifying column respectively, and the liquid phase export of 3 bottoms of nitrogen gas-liquid separation jar is maintained pipeline 4 through system's cold volume and is linked to each other with the shell side of the respective corresponding main condenser of a plurality of rectifying column respectively, and the shell side export of main condenser links to each other with heat pump 1's circulation import 5. And a first regulating valve 6 is respectively arranged between a reboiler at the lower part in the plurality of rectifying towers and a gas phase outlet of the nitrogen gas-liquid separation tank 3. The outlets of the reboilers at the lower part in the plurality of rectifying towers are respectively communicated with a system cold energy maintaining pipeline 4. The rectifying tower comprises a first rectifying tower 7 and a second rectifying tower 8; a first reboiler 9 is arranged at the inner lower part of the first rectifying tower 7, and a second reboiler 10 is arranged at the inner lower part of the second rectifying tower 8; 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 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. And a third regulating valve 16 is arranged between the shell side inlet of the main condenser and the second tee joint 13.
The invention also provides a carbon monoxide production device, 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 a raw material inlet of the first rectifying tower 7 through a raw material gas inlet 29 of the heat exchanger 19 and a raw material gas outlet 30 of the heat exchanger 19, a liquid phase outlet at the bottom of the first rectifying tower 7 is connected with a first raw material liquid inlet 20 of the second rectifying tower 8 through a sixth regulating valve 27, a gas phase outlet at the top of the second rectifying tower 8 is connected with the liquid storage tank 22 through a tube pass of the second main condenser 12, and a liquid phase outlet at the bottom of the liquid storage tank 22 is respectively connected with the product tank 18 and a second raw material liquid inlet 21 at the middle upper part of the second rectifying tower 8; a 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 circulation inlet 5 of the heat pump 1 through a second circulation gas inlet 33 of the heat exchanger 19 and a second circulation gas outlet 34 of the heat exchanger 19. 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 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 a 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:
the method comprises the following steps: the raw material gas in the raw material gas storage tank 17 sequentially passes through a raw material gas inlet 29 of the heat exchanger 19, a raw material gas outlet 30 of the heat exchanger 19 and a raw material inlet of the first rectifying tower 7 to enter the first rectifying tower 7; the feed gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: at 40 ℃ and under a pressure of: 0.7MpaG, flow: 2200 Nm/h, fraction in gas phase 1, molar fraction of carbon monoxide: 35 percent; the feed gas temperature at feed gas outlet 30 of heat exchanger 19 is: -163 ℃ 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 rectification and purification, the gas phase after primary rectification and purification enters the gas-liquid separation tank 23 through an outlet at the top of the first rectifying tower 7 and a tube pass of the first main condenser 13 to be subjected to 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 be subjected to primary rectification and purification continuously, the gas phase outlet of the gas-liquid separation tank 23 enters the waste gas furnace 25 through the first tail gas inlet 35 of the heat exchanger 19, the first tail gas outlet 36 of the heat exchanger 19 and the 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;
step three: the liquid phase purified by the primary rectification in the first step and the second step sequentially passes through a liquid phase outlet at the bottom of the first rectifying tower 7 and a sixth regulating valve 27 to enter the second rectifying tower 8 for secondary rectification and purification, the gas phase purified by the secondary rectification enters the 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 upper part of the second rectifying tower 8, and the other part of the liquid phase enters the product tank 18; the liquid phase temperature at the bottom liquid phase outlet of the first rectifying tower 7 is as follows: -165 ℃, CO purity: 69%; the product temperature in the product tank 18 is: -172 ℃ with a purity of 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 for condensation;
step five: in the third step, the waste liquid after the secondary rectification and purification through the second rectification tower 8 sequentially passes through the liquid phase outlet at the bottom of the second rectification tower 8, the fifth regulating valve 26, the second tail gas inlet 37 of the heat exchanger 19 and the second tail gas outlet 38 of the heat exchanger 19 to enter the waste gas furnace 25, and the temperature of the waste liquid at the bottom of the second rectification tower 8 is as follows: -166 ℃ and CO purity: 25%, 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 a heat exchanger 19 and a first circulating gas outlet 32 of the heat exchanger 19 to enter a nitrogen gas-liquid separation tank 3, a gas phase outlet of the nitrogen gas-liquid separation tank 3 respectively enters a first reboiler 9 and a second reboiler 10 which respectively correspond to the first reboiler 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 cycle gas temperature at the first cycle gas outlet 32 of the heat exchanger 19 is: -162 ℃; the temperature of the circulating liquid at the outlet of the first reboiler 9 was: -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 sixth step 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 respectively enters the shell pass of the first main condenser 11 and the shell pass of the second main condenser 12 to be used for maintaining the stability of the corresponding first rectifying tower 7 and the first rectifying tower 8 system, so that the influence on the purity of carbon monoxide caused by the fluctuation of the system is avoided; the circulating liquid passes through the shell side of the first main condenser 11 and the shell side of the second main condenser 12 and then returns to the heat pump 1 through a second circulating gas inlet 33, a second circulating gas outlet 34 of the heat exchanger 19 and a circulating inlet 5 of the heat pump 1; the shell-side outlet circulating gas temperature of the first main condenser 11 is as follows: -177 ℃, gas phase fraction: 0.97, the shell-side recycle 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 ℃, and the gas phase fraction: 1.
example two
The utility model provides a heat pump circulation system, includes heat pump 1, and the circulation export 2 of heat pump 1 links to each other with nitrogen gas-liquid separation jar 3 import, and the gaseous phase export at 3 tops of nitrogen gas-liquid separation jar links to each other with the reboiler of lower part in a plurality of rectifying column respectively, and the liquid phase export of 3 bottoms of nitrogen gas-liquid separation jar is maintained pipeline 4 through system's cold volume and is linked to each other with the shell side of the respective corresponding main condenser of a plurality of rectifying column respectively, and the shell side export of main condenser links to each other with heat pump 1's circulation import 5. And a first regulating valve 6 is respectively arranged between a reboiler at the lower part in the plurality of rectifying towers and a gas phase outlet of the nitrogen gas-liquid separation tank 3. The outlets of the reboilers at the lower part in the plurality of rectifying towers are respectively communicated with a system cold energy maintaining pipeline 4. The rectifying tower comprises a first rectifying tower 7 and a second rectifying tower 8; a first reboiler 9 is arranged at the inner lower part of the first rectifying tower 7, and a second reboiler 10 is arranged at the inner lower part of the second rectifying tower 8; 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 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. And a third regulating valve 16 is arranged between the shell side inlet of the main condenser and the second tee joint 13.
The invention also provides a carbon monoxide production device, 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 a raw material inlet of the first rectifying tower 7 through a raw material gas inlet 29 of the heat exchanger 19 and a raw material gas outlet 30 of the heat exchanger 19, a liquid phase outlet at the bottom of the first rectifying tower 7 is connected with a first raw material liquid inlet 20 of the second rectifying tower 8 through a sixth regulating valve 27, a gas phase outlet at the top of the second rectifying tower 8 is connected with the liquid storage tank 22 through a tube pass of the second main condenser 12, and a liquid phase outlet at the bottom of the liquid storage tank 22 is respectively connected with the product tank 18 and a second raw material liquid inlet 21 at the middle upper part of the second rectifying tower 8; a 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 circulation inlet 5 of the heat pump 1 through a second circulation gas inlet 33 of the heat exchanger 19 and a second circulation gas outlet 34 of the heat exchanger 19. 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 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 a 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:
the method comprises the following steps: the raw material gas in the raw material gas storage tank 17 sequentially passes through a raw material gas inlet 29 of the heat exchanger 19, a raw material gas outlet 30 of the heat exchanger 19 and a raw material inlet of the first rectifying tower 7 to enter the first rectifying tower 7; the feed gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: at 40 ℃ and under a pressure of: 0.7MpaG, flow: 2200 Nm/h, fraction in gas phase 1, molar fraction of carbon monoxide: 35 percent; the feed gas temperature at feed gas outlet 30 of heat exchanger 19 is: -170 ℃ 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 rectification and purification, the gas phase after primary rectification and purification enters the gas-liquid separation tank 23 through an outlet at the top of the first rectifying tower 7 and a tube pass of the first main condenser 13 to be subjected to 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 be subjected to primary rectification and purification continuously, the gas phase outlet of the gas-liquid separation tank 23 enters the waste gas furnace 25 through the first tail gas inlet 35 of the heat exchanger 19, the first tail gas outlet 36 of the heat exchanger 19 and the 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;
step three: the liquid phase purified by the primary rectification in the first step and the second step sequentially passes through a liquid phase outlet at the bottom of the first rectifying tower 7 and a sixth regulating valve 27 to enter the second rectifying tower 8 for secondary rectification and purification, the gas phase purified by the secondary rectification enters the 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 upper part of the second rectifying tower 8, and the other part of the liquid phase enters the product tank 18; the liquid phase temperature at the bottom liquid phase outlet of the first rectifying tower 7 is as follows: -170 ℃, CO purity: 75 percent; the product temperature in the product tank 18 is: 179 ℃ below zero, 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 for condensation;
step five: in the third step, the waste liquid after the secondary rectification and purification through the second rectification tower 8 sequentially passes through the liquid phase outlet at the bottom of the second rectification tower 8, the fifth regulating valve 26, the second tail gas inlet 37 of the heat exchanger 19 and the second tail gas outlet 38 of the heat exchanger 19 to enter the waste gas furnace 25, and the temperature of the waste liquid at the bottom of the second rectification tower 8 is as follows: -171 ℃, CO purity: 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 a heat exchanger 19 and a first circulating gas outlet 32 of the heat exchanger 19 to enter a nitrogen gas-liquid separation tank 3, a gas phase outlet of the nitrogen gas-liquid separation tank 3 respectively enters a first reboiler 9 and a second reboiler 10 which respectively correspond to the first reboiler 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 cycle gas temperature at the first cycle gas outlet 32 of the heat exchanger 19 is: -168 ℃; the temperature of the circulating liquid at the outlet of the first reboiler 9 was: -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 sixth step 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 respectively enters the shell pass of the first main condenser 11 and the shell pass of the second main condenser 12 to be used for maintaining the stability of the corresponding first rectifying tower 7 and the first rectifying tower 8 system, so that the influence on the purity of carbon monoxide caused by the fluctuation of the system is avoided; the circulating liquid passes through the shell side of the first main condenser 11 and the shell side of the second main condenser 12 and then returns to the heat pump 1 through a second circulating gas inlet 33, a second circulating gas outlet 34 of the heat exchanger 19 and a circulating inlet 5 of the heat pump 1; the shell-side outlet circulating gas temperature of the first main condenser 11 is as follows: -181 ℃, gas phase fraction: 0.97, the shell-side recycle 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 ℃, and the gas phase fraction: 1.
EXAMPLE III
The utility model provides a heat pump circulation system, includes heat pump 1, and the circulation export 2 of heat pump 1 links to each other with nitrogen gas-liquid separation jar 3 import, and the gaseous phase export at 3 tops of nitrogen gas-liquid separation jar links to each other with the reboiler of lower part in a plurality of rectifying column respectively, and the liquid phase export of 3 bottoms of nitrogen gas-liquid separation jar is maintained pipeline 4 through system's cold volume and is linked to each other with the shell side of the respective corresponding main condenser of a plurality of rectifying column respectively, and the shell side export of main condenser links to each other with heat pump 1's circulation import 5. And a first regulating valve 6 is respectively arranged between a reboiler at the lower part in the plurality of rectifying towers and a gas phase outlet of the nitrogen gas-liquid separation tank 3. The outlets of the reboilers at the lower part in the plurality of rectifying towers are respectively communicated with a system cold energy maintaining pipeline 4. The rectifying tower comprises a first rectifying tower 7 and a second rectifying tower 8; a first reboiler 9 is arranged at the inner lower part of the first rectifying tower 7, and a second reboiler 10 is arranged at the inner lower part of the second rectifying tower 8; 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 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. And a third regulating valve 16 is arranged between the shell side inlet of the main condenser and the second tee joint 13.
The invention also provides a carbon monoxide production device, 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 a raw material inlet of the first rectifying tower 7 through a raw material gas inlet 29 of the heat exchanger 19 and a raw material gas outlet 30 of the heat exchanger 19, a liquid phase outlet at the bottom of the first rectifying tower 7 is connected with a first raw material liquid inlet 20 of the second rectifying tower 8 through a sixth regulating valve 27, a gas phase outlet at the top of the second rectifying tower 8 is connected with the liquid storage tank 22 through a tube pass of the second main condenser 12, and a liquid phase outlet at the bottom of the liquid storage tank 22 is respectively connected with the product tank 18 and a second raw material liquid inlet 21 at the middle upper part of the second rectifying tower 8; a 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 circulation inlet 5 of the heat pump 1 through a second circulation gas inlet 33 of the heat exchanger 19 and a second circulation gas outlet 34 of the heat exchanger 19. 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 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 a 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:
the method comprises the following steps: the raw material gas in the raw material gas storage tank 17 sequentially passes through a raw material gas inlet 29 of the heat exchanger 19, a raw material gas outlet 30 of the heat exchanger 19 and a raw material inlet of the first rectifying tower 7 to enter the first rectifying tower 7; the feed gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: at 40 ℃ and under a pressure of: 0.7MpaG, flow: 2200 Nm/h, fraction in gas phase 1, molar fraction of carbon monoxide: 35 percent; the feed gas temperature at feed gas outlet 30 of heat exchanger 19 is: 166.5 ℃ below zero, gas phase fraction 1;
step two: the raw material gas entering the first rectifying tower 7 in the first step is subjected to primary rectification and purification, the gas phase after primary rectification and purification enters the gas-liquid separation tank 23 through an outlet at the top of the first rectifying tower 7 and a tube pass of the first main condenser 13 to be subjected to 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 be subjected to primary rectification and purification continuously, the gas phase outlet of the gas-liquid separation tank 23 enters the waste gas furnace 25 through the first tail gas inlet 35 of the heat exchanger 19, the first tail gas outlet 36 of the heat exchanger 19 and the 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;
step three: the liquid phase purified by the primary rectification in the first step and the second step sequentially passes through a liquid phase outlet at the bottom of the first rectifying tower 7 and a sixth regulating valve 27 to enter the second rectifying tower 8 for secondary rectification and purification, the gas phase purified by the secondary rectification enters the 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 upper part of the second rectifying tower 8, and the other part of the liquid phase enters the product tank 18; the liquid phase temperature at the bottom liquid phase outlet of the first rectifying tower 7 is as follows: 167.5 ℃ C, CO purity: 72 percent; 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 for condensation;
step five: in the third step, the waste liquid after the secondary rectification and purification through the second rectification tower 8 sequentially passes through the liquid phase outlet at the bottom of the second rectification tower 8, the fifth regulating valve 26, the second tail gas inlet 37 of the heat exchanger 19 and the second tail gas outlet 38 of the heat exchanger 19 to enter the waste gas furnace 25, and the temperature of the waste liquid at the bottom of the second rectification tower 8 is as follows: -168.5 ℃, CO purity: 27.5%, 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 a heat exchanger 19 and a first circulating gas outlet 32 of the heat exchanger 19 to enter a nitrogen gas-liquid separation tank 3, a gas phase outlet of the nitrogen gas-liquid separation tank 3 respectively enters a first reboiler 9 and a second reboiler 10 which respectively correspond to the first reboiler 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 cycle gas temperature at the first cycle gas outlet 32 of the heat exchanger 19 is: -165 ℃; the temperature of the circulating liquid at the outlet of the first reboiler 9 was: -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 sixth step 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 respectively enters the shell pass of the first main condenser 11 and the shell pass of the second main condenser 12 to be used for maintaining the stability of the corresponding first rectifying tower 7 and the first rectifying tower 8 system, so that the influence on the purity of carbon monoxide caused by the fluctuation of the system is avoided; the circulating liquid passes through the shell side of the first main condenser 11 and the shell side of the second main condenser 12 and then returns to the heat pump 1 through a second circulating gas inlet 33, a second circulating gas outlet 34 of the heat exchanger 19 and a circulating inlet 5 of the heat pump 1; the shell-side outlet circulating gas temperature of the first main condenser 11 is as follows: -179 ℃, gas phase fraction: 0.97, the shell-side recycle gas temperature of the second main condenser 12 is: -180 ℃ and 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 was 37.5 ℃, the gas phase fraction: 1.
the above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.

Claims (10)

1. A heat pump cycle system characterized by: this circulation system includes heat pump (1), the import of circulation export (2) and nitrogen gas-liquid separation jar (3) of heat pump (1) links to each other, the gaseous phase export at nitrogen gas-liquid separation jar (3) top links to each other with the reboiler of lower part in a plurality of rectifying column respectively, the liquid phase export of nitrogen gas-liquid separation jar (3) bottom is maintained pipeline (4) through system's cold volume and is linked to each other with the shell side of the respective corresponding main condenser of a plurality of rectifying column respectively, the shell side export of main condenser links to each other with circulation import (5) of heat pump (1).
2. The heat pump cycle system according to claim 1, wherein: a first regulating valve (6) is respectively arranged between a reboiler at the lower part in the plurality of rectifying towers and a gas phase outlet of the nitrogen gas-liquid separation tank (3); the outlets of the reboilers at the lower part in the plurality of rectifying towers are respectively communicated with a system cold energy maintaining pipeline (4).
3. The heat pump cycle system according to claim 1, wherein: the rectifying tower comprises a first rectifying tower (7) and a second rectifying tower (8);
a first reboiler (9) is arranged at the inner lower part of the first rectifying tower (7), and a second reboiler (10) is arranged at the inner lower part of the second rectifying tower (8);
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. The heat pump cycle system according to claim 1, wherein: a first tee joint (13) is arranged between an outlet of the reboiler and the system cold energy maintaining pipeline (4), a second tee joint (14) is arranged between a shell pass 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 heat pump cycle system according to claim 4, wherein: and a third regulating valve (16) is arranged between the shell side inlet of the main condenser and the second tee joint (13).
6. A carbon monoxide apparatus for producing, its characterized in that: the production plant comprises a feed gas storage tank (17), a product tank (18), a first rectification column (7), a first reboiler (9), a first main condenser (11), a second rectification column (8), a second reboiler (10) and a second main condenser (12) and a heat pump nitrogen circulation system according to any one of claims 1-5.
7. The carbon monoxide production apparatus according to claim 6, wherein: the feed gas storage tank (17) is connected with a feed gas inlet of the first rectifying tower (7) through a feed gas inlet (29) of the heat exchanger (19) and a feed gas outlet (30) of the heat exchanger (19), a liquid phase outlet at the bottom of the first rectifying tower (7) is connected with a first feed liquid inlet (20) of the second rectifying tower (8), a gas phase outlet at the top of the second rectifying tower (8) is connected with the liquid storage tank (22) through a tube pass of the second main condenser (12), and a liquid phase outlet at the bottom of the liquid storage tank (22) is respectively connected with the product tank (18) and a second feed liquid inlet (21) at the middle upper part of the second rectifying tower (8); a gas phase outlet at the top of the liquid storage tank (22) is connected with a tube side of the second main condenser (12);
a circulating outlet (2) of a heat pump (1) in the heat pump nitrogen circulating system is connected with an inlet of a nitrogen gas-liquid separation tank (3) through a first circulating gas inlet (31) of a heat exchanger (19) and a first circulating 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 a second circulating gas inlet (33) of the heat exchanger (19) and a second circulating gas outlet (34) of the heat exchanger (19).
8. The carbon monoxide production apparatus according to claim 7, wherein: an 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), 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 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);
and a 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).
9. The carbon monoxide production apparatus according to claim 7, 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 middle upper part of the second rectifying tower (8).
10. A production method of the carbon monoxide production apparatus as recited in claims 6 to 9, comprising the steps of:
the method comprises the following steps: raw material gas in the raw material gas storage tank (17) sequentially passes through a raw material gas inlet (29) of the heat exchanger (19), a raw material gas outlet (30) of the heat exchanger (19) and a raw material inlet of the first rectifying tower (7) and enters the first rectifying tower (7); the feed gas comprises the following components: nitrogen, hydrogen, oxygen, methane, carbon monoxide; the temperature of the feed gas is: at 40 ℃ and under a pressure of: 0.7MpaG, flow: 2200 Nm/h, fraction in gas phase 1, molar fraction of carbon monoxide: 35 percent; the raw material gas temperature of the raw material gas outlet (30) of the heat exchanger (19) is as follows: the gas phase fraction is 1 at-163 to-170 ℃;
step two: the raw material gas entering the first rectifying tower (7) in the first step is subjected to primary rectification and purification, the gas phase after primary rectification and purification enters the gas-liquid separation tank (23) through an outlet at the top of the first rectifying tower (7) and a tube pass of the first main condenser (13) to be subjected to 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 be subjected to primary rectification and purification continuously, the 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 molar fraction: 25-30%, gas phase fraction: 1;
step three: liquid phase purified by primary rectification in the first step and the second step sequentially passes through a liquid phase outlet at the bottom of the first rectifying tower (7) and a sixth regulating valve (27) and enters the second rectifying tower (8) for secondary rectification and purification, gas phase purified by secondary rectification enters the 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 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 upper part of the second rectifying tower (8), and the other part of liquid phase enters the 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 ℃, CO purity: 69-75%; the product temperature in the product tank (18) is: the purity is not lower than 99.9999 percent at the temperature of-172 to-179 ℃;
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 after the secondary rectification and purification through the second rectification tower (8) sequentially passes 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 enters the waste gas furnace (25), and the temperature of the waste liquid at the bottom of the second rectification tower (8) is as follows: -166 to-171 ℃, and the CO purity is: 25-30%, gas phase fraction: 0;
step six: circulating gas in a heat pump (1) sequentially passes through a circulating outlet (2), a first circulating gas inlet (31) of a heat exchanger (19) and a first circulating gas outlet (32) of the heat exchanger (19) and enters a nitrogen gas-liquid separation tank (3), a gas phase outlet of the nitrogen gas-liquid separation tank (3) respectively enters a first reboiler (9) and a second reboiler (10) which respectively correspond to the circulating gas through two first regulating valves (6), and the circulating gas comprises the following components: nitrogen, hydrogen, argon, nitrogen mole fraction: 99 percent; the temperature of the circulating gas at the first circulating gas outlet (32) of the heat exchanger (19) is as follows: -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: in the sixth step, a liquid phase outlet of the nitrogen gas-liquid separation tank (3) 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 respectively enters a shell pass of the first main condenser (11) and a shell pass of the second main condenser (12) to be used for maintaining the stability of the corresponding first rectifying tower (7) and the first rectifying tower (8) system, so that the influence on the purity of carbon monoxide caused by fluctuation of the system is avoided; the circulating liquid passes through the shell pass of the first main condenser (11) and the shell pass of the second main condenser (12) and then returns to the heat pump (1) through a second circulating gas inlet (33), a second circulating gas outlet (34) of the heat exchanger (19) and a circulating inlet (5) of the heat pump (1); the temperature of the shell side outlet circulating gas of the first main condenser (11) is as follows: -177 to-181 ℃, gas phase fraction: 0.97, the shell side recycle gas temperature of the second main condenser (12) is: -178 to-182 ℃, gas phase fraction: 0.99, the temperature of the circulating gas passing through a second circulating gas outlet (34) of the heat exchanger (19) is 35-40 ℃, and the gas phase fraction: 1.
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)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202010153513.1A CN111141109B (en) 2020-03-06 2020-03-06 Heat pump circulation system, carbon monoxide production device with heat pump circulation system and carbon monoxide production method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202010153513.1A CN111141109B (en) 2020-03-06 2020-03-06 Heat pump circulation system, carbon monoxide production device with heat pump circulation system and carbon monoxide production method

Publications (2)

Publication Number Publication Date
CN111141109A true CN111141109A (en) 2020-05-12
CN111141109B CN111141109B (en) 2024-03-19

Family

ID=70528457

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202010153513.1A Active CN111141109B (en) 2020-03-06 2020-03-06 Heat pump circulation system, carbon monoxide production device with heat pump circulation system and carbon monoxide production method

Country Status (1)

Country Link
CN (1) CN111141109B (en)

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
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
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

Also Published As

Publication number Publication date
CN111141109B (en) 2024-03-19

Similar Documents

Publication Publication Date Title
CN106642989B (en) Cryogenic separation system for separating mixed gas
CN104528647A (en) Method and device for preparing hydrogen and high-purity carbon monoxide by separating synthetic gas
CN104654739A (en) Device and method for preparing food-grade liquid carbon dioxide by rectification and purification with double towers
CN210625119U (en) CO cryogenic separation system capable of reducing nitrogen circulation energy consumption
CN211716982U (en) Heat pump circulation system and carbon monoxide production device with same
CN106288651B (en) With the device and production method of nitrogen heat pump rectifying production superelevation pure carbon monoxide
CN106477577B (en) A kind of device and production method of heat pump distillation production ultra-high purity carbon dioxide
CN202382516U (en) Separation and recovery device of methane and argon in synthesis ammonia relief gas
CN204702504U (en) A kind of synthetic gas is separated hydrogen making and high-purity CO device
CN110057164B (en) Production of electronic grade CO with water content less than or equal to 30ppb 2 Apparatus and method of production of (a)
CN216192118U (en) System for use coke-oven gas as raw materials production LNG and hydrogen product
CN111692838A (en) Rare gas krypton-xenon refining and ultrapure oxygen production device and production process
CN111141109B (en) Heat pump circulation system, carbon monoxide production device with heat pump circulation system and carbon monoxide production method
CN111141108B (en) Rectification purification device and purification process for liquid sulfur dioxide
CN107144092B (en) Device for producing high-purity ethylene by ethylene heat pump rectification and production process thereof
CN211625865U (en) Rectification and purification device for liquid sulfur dioxide
CN212390705U (en) Rare gas krypton-xenon refining and ultra-pure oxygen production device
CN102285658A (en) Multistage fully thermally coupled rectification production device and process method for preparing ultra-pure trichlorosilane
CN206126859U (en) Pure carbon dioxide's of heat pump distillation production superelevation device
CN215440045U (en) High-concentration phenol-ammonia wastewater double-tower energy-saving treatment system
CN212842469U (en) Single-tower cryogenic rectification argon recovery system with argon circulation and hydrogen circulation
CN210892361U (en) Device for preparing liquid carbon dioxide by utilizing surplus cold energy for refrigeration
CN210332179U (en) System for obtaining by-product hydrogen by pressure swing adsorption method in ethylene preparation process
CN219120888U (en) Device for producing ultrapure krypton-xenon by adopting krypton-xenon aspirator
CN206056114U (en) The device of superelevation pure carbon monoxide is produced with nitrogen heat pump rectification

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