CN110044133A - The apparatus and method for of separating-purifying carbon monoxide - Google Patents

The apparatus and method for of separating-purifying carbon monoxide Download PDF

Info

Publication number
CN110044133A
CN110044133A CN201910410645.5A CN201910410645A CN110044133A CN 110044133 A CN110044133 A CN 110044133A CN 201910410645 A CN201910410645 A CN 201910410645A CN 110044133 A CN110044133 A CN 110044133A
Authority
CN
China
Prior art keywords
carbon monoxide
heat exchanger
gas
knockout tower
separating
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
CN201910410645.5A
Other languages
Chinese (zh)
Other versions
CN110044133B (en
Inventor
张惊涛
王子松
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.)
Chengdu Sepmem Sci & Tech Co Ltd
Original Assignee
Chengdu Sepmem Sci & Tech 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 Chengdu Sepmem Sci & Tech Co Ltd filed Critical Chengdu Sepmem Sci & Tech Co Ltd
Priority to CN201910410645.5A priority Critical patent/CN110044133B/en
Publication of CN110044133A publication Critical patent/CN110044133A/en
Application granted granted Critical
Publication of CN110044133B publication Critical patent/CN110044133B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

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
    • 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
    • F25J2200/40—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
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/64—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end by pressure-swing adsorption [PSA] at the hot end
    • 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
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Landscapes

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

Abstract

The present invention provides a kind of apparatus and method fors of separating-purifying carbon monoxide.The equipment of separating-purifying carbon monoxide of the invention between carbon monoxide compressor and knockout tower by being arranged return line, it is back to a part compression carbon monoxide in the knockout tower as reflux carbon monoxide, this partial reflux carbon monoxide being capable of released cold quantity after carrying out reducing pressure by regulating flow, institute's chilling requirement is provided for synthesis gas cooling, cooling capacity is supplemented without additionally introducing liquid nitrogen from device external, the equipment is applicable not only to the operating condition that carbon monoxide content is high in synthesis gas and pressure is high, and the operating condition that carbon monoxide content is low suitable for synthesis gas and pressure is low, it is applied widely.The method of separating-purifying carbon monoxide of the invention is realized using above equipment, does not need additionally to introduce liquid nitrogen from device external to supplement cooling capacity in purification process, independence is strong, and applied widely, process is simple.

Description

The apparatus and method for of separating-purifying carbon monoxide
Technical field
The present invention relates to gas separation technique field more particularly to a kind of apparatus and method fors of separating-purifying carbon monoxide.
Background technique
As important carbonylation feed gas, carbon monoxide (CO) can be used for producing almost all of organic chemistry Product, such as methanol, formic acid, methylamine, acetic acid, isocyanates, ethanedioic acid, ethylene glycol, dimethyl carbonate, phosgene and pesticide herbicide Deng.
Synthesis gas is a kind of unstripped gas using carbon monoxide and hydrogen as main component, as industrial chemicals.Synthesis gas Raw material range is very wide, can be generated by solid fuel gasifications such as coal or coke, can also be by light hydrocarbons systems such as natural gas and naphthas It takes, can also be produced by heavy oil partial oxidation method.
It is all industrially the carbon monoxide for obtaining high throughput, high-purity from synthesis gas using cryogenic separation technology.It is existing Some extracts the technology of carbon monoxide and hydrogen product from synthesis gas cryogenic separation, utilizes synthesis gas pressure itself throttling drop more Pressure provides cooling capacity for unstripped gas separation, carbon monoxide.However, this method by unstripped gas form and pressure limit, when from Status from carbon monoxide reducing pressure by regulating flow provide cooling capacity deficiency when, pass through filling liquid nitrogen supplement cooling capacity, this mode very great Cheng Its application range is limited on degree, it is some without air separation unit, without the factory of liquid nitrogen product, the method is just difficult to realize, In other words, it is existing it is this from the method for synthesis gas purification & isolation carbon monoxide have it is small to unstripped gas adaptation range, excessive Rely on liquid nitrogen, the disadvantages of energy consumption is high.
It thus develops and a kind of be suitable for various unstripped gas conditions, do not need that liquid nitrogen, low energy consumption, the simple carbon monoxide of process Cryogenic separation purification technique is particularly significant.
Summary of the invention
The purpose of the present invention, which first consists in, provides a kind of equipment of separating-purifying carbon monoxide, using the equipment from synthesis gas When carbon monoxide is produced in middle purification, do not need additionally to introduce liquid nitrogen from device external to supplement cooling capacity, independence is strong, the scope of application Extensively.
The object of the invention is also to provide a kind of methods of separating-purifying carbon monoxide, and volume is not needed in purification process Liquid nitrogen is introduced to supplement cooling capacity from device external outside, and independence is strong, and applied widely, process is simple.
In order to achieve the above object, present invention firstly provides a kind of equipment of separating-purifying carbon monoxide, including pass through pipeline Heat exchanger, the first gas-liquid separator, knockout tower, the second gas-liquid separator and the carbon monoxide compressor being sequentially communicated；
In pipeline between the knockout tower and second gas-liquid separator be equipped with throttle valve, the throttle valve for pair Fluid carries out reducing pressure by regulating flow cooling；
The first heat exchanger channels and the second heat exchanger channels are equipped in the heat exchanger, first heat exchanger channels are for making to synthesize Gas passes through and cools down to it, and second heat exchanger channels are for making to flow out from the knockout tower and carrying out reducing pressure by regulating flow cooling Fluid afterwards passes through with released cold quantity；
Return line is equipped between the carbon monoxide compressor and the knockout tower, the return line is described for making A part compression carbon monoxide is back in the knockout tower as reflux carbon monoxide in carbon monoxide compressor；The heat exchange Third heat exchanger channels are equipped in device, the third heat exchanger channels are located in the return line, for flow back carbon monoxide from In by when it is cooled down.
In some embodiments of the invention, the tower bottom of the knockout tower is equipped with reboiler.
In some embodiments of the invention, the return line is connected to the entrance of the reboiler, the reboiler Outlet by pipeline connection to the top or middle part of the knockout tower.
In some embodiments of the invention, the return line is connected to the top or middle part of the knockout tower；
First heat exchanger channels include discontinuous first heat exchanging segment and the second heat exchanging segment, and first heat exchanging segment goes out For mouth by the entrance of pipeline connection to the reboiler, the outlet of the reboiler passes through pipeline connection to second heat exchanging segment Entrance, the outlet of second heat exchanging segment passes through pipeline connection to first gas-liquid separator.
In some embodiments of the invention, the equipment of the separating-purifying carbon monoxide further includes the first forecooler, institute The first forecooler is stated set on the upstream of the heat exchanger and is connected to by pipeline with the heat exchanger.
In some embodiments of the invention, the equipment of the separating-purifying carbon monoxide further includes the second forecooler, institute The second forecooler is stated in the return line, and the third for being set to the carbon monoxide compressor and the heat exchanger exchanges heat Between channel.
In some embodiments of the invention, multiple reducing pressure by regulating flow pipes are equipped between the knockout tower and the heat exchanger Road is equipped with throttle valve in each reducing pressure by regulating flow pipeline；
Multiple second heat exchanger channels are equipped in the heat exchanger, the multiple second heat exchanger channels respectively correspond described in connection Multiple reducing pressure by regulating flow pipelines.
In some embodiments of the invention, the equipment of the separating-purifying carbon monoxide further includes being set to the heat exchanger The purification device of upstream.
In some embodiments of the invention, the 4th heat exchanger channels and the 5th heat exchanger channels, institute are equipped in the heat exchanger The top of the 4th heat exchanger channels and first gas-liquid separator is stated by pipeline connection, the 5th heat exchanger channels with described point From passing through pipeline connection at the top of tower.
The present invention also provides a kind of methods of separating-purifying carbon monoxide, using the equipment of above-mentioned separating-purifying carbon monoxide It realizes, which comprises
The first heat exchanger channels for making synthesis gas enter the heat exchanger cool down, and the synthesis gas partial condensation becomes the One gas-liquid mixture；
First gas-liquid mixture, which enters in first gas-liquid separator, carries out gas-liquid separation, is formed and is located at described First liquid phase of the first gas-liquid separator bottom and the first gas phase above first liquid phase, first gas phase from The top of first gas-liquid separator escapes；
Enter first liquid phase in the knockout tower, the gas of the rising of first liquid phase and the knockout tower tower bottom Phase counter current contacting, finally obtains the second liquid phase positioned at tower bottom and the second gas phase positioned at tower top, and second gas phase is from tower Top evolution；
The second liquid phase carries out reducing pressure by regulating flow cooling, shape after the outflow of the tower bottom of the knockout tower, through the throttle valve At the second gas-liquid mixture；
Second gas-liquid mixture is set to enter the third heat exchanger channels released cold quantity of the heat exchanger, second gas-liquid Mixture is all evaporated to CO gas, enters CO gas in carbon monoxide compressor and is compressed；
A part compression carbon monoxide is extracted from the carbon monoxide compressor as reflux carbon monoxide enters reflux Pipeline, the reflux carbon monoxide enter in the knockout tower after the cooling of the third heat exchanger channels of the heat exchanger.
Beneficial effects of the present invention:
The equipment of separating-purifying carbon monoxide of the invention between carbon monoxide compressor and knockout tower by being arranged back Flow tube road is back to a part compression carbon monoxide in the knockout tower as reflux carbon monoxide, this one oxygen of partial reflux Change carbon after carrying out reducing pressure by regulating flow can released cold quantity, for synthesis gas cool down institute's chilling requirement is provided, do not need additionally outside equipment Portion introduces liquid nitrogen to supplement cooling capacity, and equipment of the invention is applicable not only to the work that carbon monoxide content is high in synthesis gas and pressure is high Condition, and the operating condition that carbon monoxide content is low suitable for synthesis gas and pressure is low, it is applied widely.
The method of separating-purifying carbon monoxide of the invention is by extracting a part compression carbon monoxide as one oxygen of reflux Change carbon to flow back into knockout tower, capable of cooling down after the progress reducing pressure by regulating flow cooling of this partial reflux carbon monoxide for synthesis gas, it is cold to provide Amount does not need additionally to introduce liquid nitrogen from device external to supplement cooling capacity, and this method is applicable not only to carbon monoxide in synthesis gas and contains The operating condition that amount is high and pressure is high, and the operating condition that carbon monoxide content is low suitable for synthesis gas and pressure is low, with traditional one Carbonoxide low temperature separating process is compared, and the independence of this method is strong, and applied widely, process is simple.In addition, flowing back in the present invention After carbon monoxide enters knockout tower from the top of knockout tower or middle part, the liquid phase flow in knockout tower can be increased, promote washing Effect, and then improve the rate of recovery of carbon monoxide.
Detailed description of the invention
In order to illustrate the technical solution of the embodiments of the present invention more clearly, below will be to needed in the embodiment attached Figure is briefly described, it should be understood that the following drawings illustrates only certain embodiments of the present invention, therefore is not construed as pair The restriction of range for those of ordinary skill in the art without creative efforts, can also be according to this A little attached drawings obtain other relevant attached drawings.
Fig. 1 is the structural schematic diagram of the first embodiment of the equipment of separating-purifying carbon monoxide of the invention；
Fig. 2 is the structural schematic diagram of the second embodiment of the equipment of separating-purifying carbon monoxide of the invention.
Main element symbol description:
10, purification device；21, the first forecooler；30, heat exchanger；31, the first heat exchanger channels；311, the first heat exchanging segment； 312, the second heat exchanging segment；32, the second heat exchanger channels；33, third heat exchanger channels；34, the 4th heat exchanger channels；35, the 5th heat exchange is logical Road；41, the first gas-liquid separator；50, knockout tower；51, reboiler；42, the second gas-liquid separator；60, throttle valve；70, an oxygen Change carbon compressor；72, intercooler；22, the second forecooler.
Specific embodiment
The embodiment of the present invention is described below in detail, examples of the embodiments are shown in the accompanying drawings, wherein from beginning to end Same or similar label indicates same or similar element or element with the same or similar functions.Below with reference to attached The embodiment of figure description is exemplary, and for explaining only the invention, and is not considered as limiting the invention.
In the description of the present invention, it is to be understood that, term " center ", " longitudinal direction ", " transverse direction ", " length ", " width ", " thickness ", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outside", " up time The orientation or positional relationship of the instructions such as needle ", " counterclockwise ", " axial direction ", " radial direction ", " circumferential direction " be orientation based on the figure or Positional relationship is merely for convenience of description of the present invention and simplification of the description, rather than the device or element of indication or suggestion meaning must There must be specific orientation, be constructed and operated in a specific orientation, therefore be not considered as limiting the invention.
In addition, term " first ", " second " are used for descriptive purposes only and cannot be understood as indicating or suggesting relative importance Or implicitly indicate the quantity of indicated technical characteristic.Define " first " as a result, the feature of " second " can be expressed or Implicitly include one or more of the features.In the description of the present invention, the meaning of " plurality " is two or more, Unless otherwise specifically defined.
In the present invention unless specifically defined or limited otherwise, term " installation ", " connected ", " connection ", " fixation " etc. Term shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or integral；It can be mechanical connect It connects, is also possible to be electrically connected；It can be directly connected, can also can be in two elements indirectly connected through an intermediary The interaction relationship of the connection in portion or two elements.It for the ordinary skill in the art, can be according to specific feelings Condition understands the concrete meaning of above-mentioned term in the present invention.
In the present invention unless specifically defined or limited otherwise, fisrt feature in the second feature " on " or " down " can be with It is that the first and second features directly contact or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists Second feature " on ", " top " and " above " but fisrt feature be directly above or diagonally above the second feature, or be merely representative of First feature horizontal height is higher than second feature.Fisrt feature can be under the second feature " below ", " below " and " below " One feature is directly under or diagonally below the second feature, or is merely representative of first feature horizontal height less than second feature.
Fig. 1 and Fig. 2 are please referred to, present invention firstly provides a kind of equipment of separating-purifying carbon monoxide, including pass through pipeline Heat exchanger 30, the first gas-liquid separator 41, knockout tower 50, the second gas-liquid separator 42 and the carbon monoxide compression being sequentially communicated Machine 70；
Throttle valve 60, the throttle valve are equipped in pipeline between the knockout tower 50 and second gas-liquid separator 42 60 for carrying out reducing pressure by regulating flow cooling to fluid；
The first heat exchanger channels 31 and the second heat exchanger channels 32 are equipped in the heat exchanger 30, first heat exchanger channels 31 are used In passing through synthesis gas and cool down to it, second heat exchanger channels 32 are flowed out and are carried out from the knockout tower 50 for making Fluid after reducing pressure by regulating flow cooling passes through with released cold quantity；
Return line is equipped between the carbon monoxide compressor 70 and the knockout tower 50, the return line is for making A part compression carbon monoxide is back in the knockout tower 50 as reflux carbon monoxide in the carbon monoxide compressor 70； Third heat exchanger channels 33 are equipped in the heat exchanger 30, the third heat exchanger channels 33 are located in the return line, are used for Reflux carbon monoxide cools down it when passing therethrough.
The course of work of the equipment of separating-purifying carbon monoxide of the invention is substantially are as follows:
A. after the first heat exchanger channels 31 that synthesis gas enters the heat exchanger 30 carry out cooling, temperature reduction leads to part gas Body condensation forms the first gas-liquid mixture, and it is to make to synthesize as far as possible that the synthesis gas, which enters the cooling purpose of the heat exchanger 30, All carbon monoxide in gas are condensed into liquid, provide basis for later separation.
Specifically, the temperature for the first gas-liquid mixture that synthesis gas is formed after first heat exchanger channels 31 are cooling It is -170 DEG C~-190 DEG C.
B. first gas-liquid mixture, which enters in first gas-liquid separator 41, carries out gas-liquid separation, is formed and is located at The first liquid phase and the first gas phase above first liquid phase of first gas-liquid separator, 41 bottom, described first Gas phase is escaped from the top of first gas-liquid separator 41, specifically, first gas phase is mainly hydrogen, while being mingled with few Measure carbon monoxide.
Enter first liquid phase in the knockout tower 50, the hydrogen after tower bottom is heated, in first liquid phase Gas switchs to gaseous state from liquid, forms the second gas phase, and second gas phase is escaped from the tower top of the knockout tower 50, and liquid one aoxidizes Carbon remaines in the tower bottom of the knockout tower 50, forms second liquid phase, second gas phase is mainly hydrogen, while being mingled with a small amount of one Carbonoxide.
D. the second liquid phase carries out reducing pressure by regulating flow drop through the throttle valve 60 after the outflow of the tower bottom of the knockout tower 50 Temperature forms the second gas-liquid mixture of low-temp low-pressure, and the temperature of the second gas-liquid mixture is -140 DEG C~-180 DEG C, when the second gas When the third heat exchanger channels 33 that liquid mixture is directly entered heat exchanger 30 are cooled down, due to the gas in the second gas-liquid mixture Being easy to converge to above liquid causes gas-liquid mixed uneven, and since gas is different from the cooling capacity that liquid carries, straight It connects that the second gas-liquid mixture is passed through heat exchanger 30 and is exchanged heat and will appear the non-uniform problem of heat exchange, to avoid the occurrence of the problem, this Invention is provided with the second gas-liquid separator 42, again respectively according to constant after gas and the liquid in the second gas-liquid mixture are separated Rate be passed through in the third heat exchanger channels 33 of the heat exchanger 30, guarantee that gas and liquid are uniformly mixed, realization is uniformly changed Thermal effect.
E. second gas-liquid mixture is by the way that itself is by re-heat when 33 released cold quantity of third heat exchanger channels, institute at this time It states the second gas-liquid mixture and all switchs to CO gas, CO gas enters carbon monoxide compressor 70 and pressed later It shortens into as carbon monoxide product.
F. in order to which the equipment for making separating-purifying carbon monoxide of the invention can be realized cooling capacity self-sufficiency, the section of step d is avoided The cooling capacity that stream decompression cooling link generates is not able to satisfy the demand that synthesis gas cools down in step a, and the present invention, which is also provided with, to be made to flow back Carbon monoxide is back to the return line in the knockout tower 50, and the purpose that the return line is arranged is: can increase and be used for The amount of the carbon monoxide stream of reducing pressure by regulating flow increases the cooling capacity of reducing pressure by regulating flow link release, is synthesis gas cooling in heat exchanger 30 (condensation) provides enough cooling capacity.
In the prior art, in the case where unstripped gas CO content is lower or the lower situation of raw gas pressure, CO liquid throttling drop It is impossible to meet the needs of synthesis air cooling (condensation), the present invention is returned the cooling capacity generated after pressure by extracting compressed part CO Stream supplements insufficient cooling capacity using the principle of compression refrigeration for synthesis air cooling (condensation).
The present invention provides difference scarce cooling capacity using circulation CO, can also make under the operating condition that unstripped gas CO content is low, pressure is low Equipment, which operates normally, to be applicable in, and does not need additionally to supplement liquid nitrogen, technique independence is strong, applied widely.
In some embodiments of the invention, the heat exchanger 30 is plate-fin heat exchanger 30.
Specifically, the reflux carbon monoxide can be carbon monoxide product, or extracted out in advance in compression process The carbon monoxide lower than carbon monoxide product pressure, alternatively, in order to meet supplement cooling capacity and low energy consumption needs, the reflux Carbon monoxide may be the carbon monoxide that pressure is greater than carbon monoxide product, this just needs reaching carbon monoxide product pressure After be further added by number of compression stages, the carbon monoxide that is refluxed will be needed to be compressed to higher pressure.The temperature of the reflux carbon monoxide Degree is 30 DEG C~40 DEG C.
In the present invention, the pressure of carbon monoxide product can need to be adjusted according to downstream user, and flow back carbon monoxide The number of cooling capacity that can supplement as needed of pressure and energy consumption minimum principle be adjusted, flexible and convenient operation.
Specifically, as shown in Figures 1 and 2, the tower bottom of the knockout tower 50 is equipped with reboiler 51, and the reboiler 51 is used for Tower bottoms (i.e. second liquid phase) is heated, so that remaining hydrogen is switched to gaseous state from liquid, then from described point Tower top evolution from tower 50.
In some embodiments of the invention, the reboiler 51 is soaked in the liquid (i.e. second liquid phase) of tower bottom, heat Medium (synthesis gas or reflux carbon monoxide) flowing is heated inside the reboiler 51 to the liquid to tower bottom.
As shown in Figure 1, in the first embodiment of the present invention, the return line is connected to entering for the reboiler 51 Mouthful, the outlet of the reboiler 51 passes through pipeline connection to the top or middle part of the knockout tower 50.In this first embodiment, Reflux carbon monoxide enters described point from tower top again later first by the reboiler 51 to supply tower bottom heating institute's calorific requirement From tower 50, is finally flowed out from tower bottom and carry out reducing pressure by regulating flow cooling.
As shown in Fig. 2, the return line is connected to the top of the knockout tower 50 in the second embodiment of the present invention Or middle part, in the second embodiment, providing the fluid of heat for 50 tower bottom of knockout tower is synthesis gas.
In this second embodiment, first heat exchanger channels 31 include that discontinuous first heat exchanging segment 311 is changed with second The outlet of hot arc 312, first heat exchanging segment 311 passes through entrance of the pipeline connection to the reboiler 51, the reboiler 51 Outlet by the entrance of pipeline connection to second heat exchanging segment 312, the outlet of second heat exchanging segment 312 passes through pipeline company Pass to first gas-liquid separator 41.
In the second embodiment, reflux carbon monoxide, which enters after the knockout tower 50, directly carries out throttling drop from tower bottom outflow Pressure drop temperature.Synthesis gas initially enters first heat exchanging segment 311 and carries out first time cooling, boils again via pipeline into described later Tower bottoms is heated in device 51, is carried out after the reboiler 51 outflow through entering second heat exchanging segment 312 by pipeline Second of cooling.Specifically, it is -170 DEG C~-190 DEG C that the synthesis gas, which carries out the temperature after cooling down second,.
Specifically, the temperature of the tower bottom of the knockout tower 50 is -160 DEG C~-180 DEG C, the temperature of tower top is -170 DEG C~- 200℃。
Preferably, as shown in Figure 1, the equipment of the separating-purifying carbon monoxide further includes the first forecooler 21, described One forecooler 21 is set to the upstream of the heat exchanger 30 and is connected to by pipeline with the heat exchanger 30.First forecooler 21 are pre-chilled it for entering before heat exchanger 30 cools down in synthesis gas, and the temperature after the synthesis gas pre-cooling is 0 DEG C~-30 DEG C, such as 0 DEG C, -5 DEG C, -10 DEG C, -15 DEG C, -20 DEG C, -25 DEG C, -30 DEG C.
Preferably, as shown in Figure 1, the equipment of the separating-purifying carbon monoxide further includes the second forecooler 22, described Two forecoolers 22 are set in the return line, and are changed set on the carbon monoxide compressor 70 and the third of the heat exchanger 30 Between the passage of heat 33.First forecooler 21 be used for reflux carbon monoxide enter before heat exchanger 30 cools down it is carried out it is pre- Cold, the temperature after the carbon monoxide pre-cooling is 0 DEG C~-30 DEG C, such as 0 DEG C, -5 DEG C, -10 DEG C, -15 DEG C, -20 DEG C, -25 ℃、-30℃。
The first forecooler 21 is arranged in the present invention and the purpose of the second forecooler 22 is to reduce the amount of reflux carbon monoxide, drop The compression energy consumption (about 20~30%) of low CO saves production cost.
Specifically, the reducing pressure by regulating flow can divide multistage progress, and in other words, the knockout tower 50 and the heat exchanger 30 Between be equipped with multiple reducing pressure by regulating flow pipelines, throttle valve 60 is equipped in each reducing pressure by regulating flow pipeline, from 50 tower bottom of knockout tower The second liquid phase (i.e. liquid CO) of outflow is entered in the heat exchanger 30 by multiple-limb pipeline, so as to multiple Reducing pressure by regulating flow is carried out to liquid CO in reducing pressure by regulating flow pipeline, enables the carbon monoxide for being down to different pressures different Warm area released cold quantity.
In some embodiments of the invention, multiple second heat exchanger channels 32 are equipped in the heat exchanger 30, it is the multiple Second heat exchanger channels 32 respectively correspond the multiple reducing pressure by regulating flow pipeline of connection.
In addition, can be dropped in multiple throttlings by being respectively controlled to the throttle valve 60 in multiple reducing pressure by regulating flow pipelines Different decompression cooling effects is realized in pressure pipe road, to meet the refrigeration requirement of the second heat exchanger channels 32 of different temperatures grade.
As shown in Figures 1 and 2, in some embodiments of the invention, the carbon monoxide compressor 70 has multiple pressures Contracting series, the suction inlet of the multiple compression stage are respectively communicated with the multiple second heat exchanger channels 32, are respectively used to from described The CO gas that multiple second heat exchanger channels 32 flow out is compressed.In some embodiments of the invention, an oxygen Change and is equipped with multiple intercoolers 72 between multiple compression stages of carbon compressor 70.
As shown in Figures 1 and 2, in one embodiment of this invention, 2 grades of progress of the reducing pressure by regulating flow point, from the separation The liquid CO of 50 tower bottom of tower outflow is entered in the heat exchanger 30 by 2 reducing pressure by regulating flow pipelines, the heat exchanger 30 In be equipped with 2 the second heat exchanger channels 32,2 second heat exchanger channels 32 are respectively communicated with 2 reducing pressure by regulating flow pipelines.It is described Carbon monoxide compressor 70 has 2 grades of air entries, and 2 air entries are respectively used to from 2 second heat exchanger channels 32 The CO gas of outflow is sucked and is compressed.
Preferably, the equipment of the separating-purifying carbon monoxide further includes the purification device set on 30 upstream of heat exchanger 10, the purification device 10 is used to carry out purified treatment to synthesis gas before synthesis gas enters heat exchanger 30, removes the synthesis The objectionable impurities for being easy to cause equipment frozen block under equipment or low temperature, such as carbon dioxide, methanol, water, sulphur are easily corroded in gas Compound and mercury etc..
In some embodiments of the invention, the 4th heat exchanger channels 34 and the 5th heat exchanger channels are equipped in the heat exchanger 30 35, by pipeline connection, the 5th heat exchange is logical at the top of the 4th heat exchanger channels 34 and first gas-liquid separator 41 The top of road 35 and the knockout tower 50 passes through pipeline connection.The first gas phase escaped at the top of first gas-liquid separator 41 Itself cooling capacity is discharged after into the 4th heat exchanger channels 34, to need cooled synthesis gas to provide in the first heat exchanger channels 31 Cooling capacity is discharged after itself re-heat；After the second gas phase escaped at the top of the knockout tower 50 enters the 5th heat exchanger channels 35 Itself cooling capacity is discharged, to need cooled synthesis gas to provide cooling capacity in the first heat exchanger channels 31, is discharged after itself re-heat.
In some embodiments of the invention, the equipment of the separating-purifying carbon monoxide further includes and the heat exchanger 30 By pressure-variable adsorption (PSA) device of pipeline connection, the pressure-swing absorption apparatus is connected to the 4th heat exchanger channels 34, is used for Separating-purifying is carried out to the first gas phase, CO gas a small amount of in the first gas phase is removed, to obtain the hydrogen of high-purity.
The equipment of separating-purifying carbon monoxide of the invention between carbon monoxide compressor 70 and knockout tower 50 by setting Return line is set, is back to a part compression carbon monoxide in the knockout tower 50 as reflux carbon monoxide, this part is returned Flow carbon monoxide after carrying out reducing pressure by regulating flow can released cold quantity, for synthesis gas cooling institute's chilling requirement is provided, do not need additionally from Device external introduces liquid nitrogen to supplement cooling capacity, and equipment of the invention is applicable not only to carbon monoxide content height and pressure in synthesis gas High operating condition, and the operating condition that carbon monoxide content is low suitable for synthesis gas and pressure is low, it is applied widely.
Based on the equipment of above-mentioned separating-purifying carbon monoxide, the present invention also provides a kind of sides of separating-purifying carbon monoxide Method is realized using the equipment of above-mentioned separating-purifying carbon monoxide, which comprises
Make synthesis gas enter the heat exchanger 30 the first heat exchanger channels 31 cool down, the synthesis gas partial condensation at For the first gas-liquid mixture；
First gas-liquid mixture, which enters in first gas-liquid separator 41, carries out gas-liquid separation, is formed and is located at institute The first liquid phase and the first gas phase above first liquid phase for stating 41 bottom of the first gas-liquid separator, first gas Mutually escaped from the top of first gas-liquid separator 41；
Enter first liquid phase in the knockout tower 50, the rising of first liquid phase and 50 tower bottom of knockout tower Gas phase counter current contacting, finally obtain the second liquid phase positioned at tower bottom and the second gas phase positioned at tower top, second gas phase It is escaped from tower top；
The second liquid phase carries out reducing pressure by regulating flow drop after the outflow of the tower bottom of the knockout tower 50, through the throttle valve 60 Temperature forms the second gas-liquid mixture；
Make second gas-liquid mixture enter the heat exchanger 30 33 released cold quantity of third heat exchanger channels, described second Gas-liquid mixture is all evaporated to CO gas, enters CO gas in carbon monoxide compressor 70 and is compressed；
A part compression carbon monoxide is extracted from the carbon monoxide compressor 70 to enter back as reflux carbon monoxide Flow tube road, the reflux carbon monoxide enter the knockout tower 50 after the third heat exchanger channels 33 of the heat exchanger 30 cool down In.
Specifically, when the pressure of first liquid phase is larger, it can be in first gas-liquid separator 41 and described point First liquid phase is depressured from throttle valve 60 is arranged on the pipeline between tower 50, makes the pressure drop of first liquid phase It is low, to meet the operating pressure requirement inside the knockout tower 50.
In the embodiment shown in fig. 1, the return line is connected to the entrance of the reboiler 51, the reboiler 51 Outlet by pipeline connection to the top or middle part of the knockout tower 50, in the return line reflux carbon monoxide first into Enter the reboiler 51 to heat tower bottoms, through entering the knockout tower 50 by pipeline after the reboiler 51 outflow It is interior.
In the embodiment shown in Figure 2, the return line is connected to the top or middle part of the knockout tower 50, reflux one Carbonoxide is directly entered in the knockout tower 50 after return line outflow.
First heat exchanger channels 31 include discontinuous first heat exchanging segment 311 and the second heat exchanging segment 312, and described first changes By pipeline connection to the entrance of the reboiler 51, the outlet of the reboiler 51 passes through pipeline connection for the outlet of hot arc 311 To the entrance of second heat exchanging segment 312, the outlet of second heat exchanging segment 312 passes through pipeline connection to first gas-liquid point From device 41；Synthesis gas initially enters first heat exchanging segment 311 and carries out first time cooling, boils again via pipeline into described later Tower bottoms is heated in device 51, is carried out after the reboiler 51 outflow through entering second heat exchanging segment 312 by pipeline Second of cooling.After cooling down for the second time, the synthesis gas for being cooled to certain temperature (- 140 DEG C~-160 DEG C) enters reboiler 51 In for tower bottom heating institute's calorific requirement is provided.
As can be seen that the carbon monoxide that flows back is from the top or middle part of the knockout tower 50 in the embodiment of Fig. 1 and Fig. 2 Into in the knockout tower 50, during the carbon monoxide that flows back flow to tower bottom from the top of the knockout tower 50 or middle part, This partial reflux carbon monoxide can increase the liquid phase flow in knockout tower 50, reinforce the mass transport process of gas-liquid two-phase, make second Carbon monoxide in gas phase can be more preferably recycled in second liquid phase, enhance rectification effect.
The method of separating-purifying carbon monoxide of the invention is by extracting a part compression carbon monoxide as one oxygen of reflux Change carbon to flow back into knockout tower 50, this partial reflux carbon monoxide can provide after carrying out reducing pressure by regulating flow cooling for synthesis gas cooling Cooling capacity does not need additionally to introduce liquid nitrogen from device external to supplement cooling capacity, and this method is applicable not only to carbon monoxide in synthesis gas The operating condition that content is high and pressure is high, and the operating condition that carbon monoxide content is low suitable for synthesis gas and pressure is low are and traditional Carbon monoxide under low temperature separating technology is compared, and the independence of this method is strong, and applied widely, process is simple.In addition, being returned in the present invention After flow carbon monoxide enters knockout tower 50, the liquid phase flow in knockout tower 50 can be increased, promote washing effect, and then improve one The rate of recovery of carbonoxide.
Herein, " upstream ", " downstream " refer to the circulation path of synthesis gas, in separating-purifying carbon monoxide of the invention Method in, synthesis gas is from upstream to downstream flow.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show The description of example " or " some examples " etc. means specific features, structure, material or spy described in conjunction with this embodiment or example Point is included at least one embodiment or example of the invention.In the present specification, schematic expression of the above terms are not It must be directed to identical embodiment or example.Moreover, particular features, structures, materials, or characteristics described can be in office It can be combined in any suitable manner in one or more embodiment or examples.In addition, without conflicting with each other, the skill of this field Art personnel can tie the feature of different embodiments or examples described in this specification and different embodiments or examples It closes and combines.
Although the embodiments of the present invention has been shown and described above, it is to be understood that above-described embodiment is example Property, it is not considered as limiting the invention, those skilled in the art within the scope of the invention can be to above-mentioned Embodiment is changed, modifies, replacement and variant.

Claims (10)

1. a kind of equipment of separating-purifying carbon monoxide, which is characterized in that including be sequentially communicated by pipeline heat exchanger, first Gas-liquid separator, knockout tower, the second gas-liquid separator and carbon monoxide compressor；
Throttle valve is equipped in pipeline between the knockout tower and second gas-liquid separator, the throttle valve is used for fluid Carry out reducing pressure by regulating flow cooling；
The first heat exchanger channels and the second heat exchanger channels are equipped in the heat exchanger, first heat exchanger channels are for keeping synthesis gas logical It crosses and it is cooled down, second heat exchanger channels are for making after flowing out from the knockout tower and carrying out reducing pressure by regulating flow cooling Fluid passes through with released cold quantity；
Return line is equipped between the carbon monoxide compressor and the knockout tower, the return line is for making an oxygen Change a part compression carbon monoxide in carbon compressor to be back in the knockout tower as reflux carbon monoxide；In the heat exchanger Equipped with third heat exchanger channels, the third heat exchanger channels are located in the return line, for therefrom leading in reflux carbon monoxide It is out-of-date that it is cooled down.
2. the equipment of separating-purifying carbon monoxide as described in claim 1, which is characterized in that the tower bottom of the knockout tower is equipped with Reboiler.
3. the equipment of separating-purifying carbon monoxide as claimed in claim 2, which is characterized in that the return line is connected to institute The entrance of reboiler is stated, the outlet of the reboiler passes through pipeline connection to the top or middle part of the knockout tower.
4. the equipment of separating-purifying carbon monoxide as claimed in claim 2, which is characterized in that the return line is connected to institute State the top or middle part of knockout tower；
First heat exchanger channels include discontinuous first heat exchanging segment and the second heat exchanging segment, and the outlet of first heat exchanging segment is logical The entrance of pipeline connection to the reboiler is crossed, the outlet of the reboiler passes through pipeline connection entering to second heat exchanging segment Mouthful, the outlet of second heat exchanging segment passes through pipeline connection to first gas-liquid separator.
5. the equipment of separating-purifying carbon monoxide as described in claim 1, which is characterized in that further include the first forecooler, institute The first forecooler is stated set on the upstream of the heat exchanger and is connected to by pipeline with the heat exchanger.
6. the equipment of separating-purifying carbon monoxide as described in claim 1, which is characterized in that further include the second forecooler, institute The second forecooler is stated in the return line, and the third for being set to the carbon monoxide compressor and the heat exchanger exchanges heat Between channel.
7. the equipment of separating-purifying carbon monoxide as described in claim 1, which is characterized in that the knockout tower and the heat exchange It is equipped with multiple reducing pressure by regulating flow pipelines between device, is equipped with throttle valve in each reducing pressure by regulating flow pipeline；
Multiple second heat exchanger channels are equipped in the heat exchanger, it is the multiple that the multiple second heat exchanger channels respectively correspond connection Reducing pressure by regulating flow pipeline.
8. the equipment of separating-purifying carbon monoxide as described in claim 1, which is characterized in that further include being set to the heat exchanger The purification device of upstream.
9. the equipment of separating-purifying carbon monoxide as described in claim 1, which is characterized in that be equipped with the 4th in the heat exchanger The top of heat exchanger channels and the 5th heat exchanger channels, the 4th heat exchanger channels and first gas-liquid separator is connected by pipeline It is logical, pass through pipeline connection at the top of the 5th heat exchanger channels and the knockout tower.
10. a kind of method of separating-purifying carbon monoxide, which is characterized in that use as described in any one of claim 1 to 9 point Equipment from purifying carbon oxide is realized, which comprises
The first heat exchanger channels for making synthesis gas enter the heat exchanger cool down, and the synthesis gas partial condensation becomes the first gas Liquid mixture；
First gas-liquid mixture, which enters in first gas-liquid separator, carries out gas-liquid separation, is formed and is located at described first First liquid phase of gas-liquid separator bottom and the first gas phase above first liquid phase, first gas phase is from described The top of first gas-liquid separator escapes；
Enter first liquid phase in the knockout tower, the gas-phase reverse of the rising of first liquid phase and the knockout tower tower bottom Stream contact, finally obtains the second liquid phase positioned at tower bottom and the second gas phase positioned at tower top, and second gas phase is escaped from tower top Out；
The second liquid phase carries out reducing pressure by regulating flow cooling after the outflow of the tower bottom of the knockout tower, through the throttle valve, forms the Two gas-liquid mixtures；
Second gas-liquid mixture is set to enter the third heat exchanger channels released cold quantity of the heat exchanger, second gas-liquid mixed Object is all evaporated to CO gas, enters CO gas in carbon monoxide compressor and is compressed；
A part compression carbon monoxide is extracted from the carbon monoxide compressor as reflux carbon monoxide enters return line, The reflux carbon monoxide enters in the knockout tower after the cooling of the third heat exchanger channels of the heat exchanger.
CN201910410645.5A 2019-05-17 2019-05-17 Apparatus and method for separating and purifying carbon monoxide Active CN110044133B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201910410645.5A CN110044133B (en) 2019-05-17 2019-05-17 Apparatus and method for separating and purifying carbon monoxide

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201910410645.5A CN110044133B (en) 2019-05-17 2019-05-17 Apparatus and method for separating and purifying carbon monoxide

Publications (2)

Publication Number Publication Date
CN110044133A true CN110044133A (en) 2019-07-23
CN110044133B CN110044133B (en) 2024-03-22

Family

ID=67282348

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201910410645.5A Active CN110044133B (en) 2019-05-17 2019-05-17 Apparatus and method for separating and purifying carbon monoxide

Country Status (1)

Country Link
CN (1) CN110044133B (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112090106A (en) * 2020-09-15 2020-12-18 中国地质大学（武汉） Reagent purification device and method for purifying ammonium bifluoride or ammonium fluoride by using same

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4805414A (en) * 1987-12-15 1989-02-21 Union Carbide Corporation Process to recover hydrogen-free higher boiling synthesis gas component
CN101627273A (en) * 2006-11-30 2010-01-13 林德股份公司 Method and device for obtaining products from synthesis gas
CN204006964U (en) * 2014-07-01 2014-12-10 开封空分集团有限公司 The device of Deep Cooling Method making pure carbon monoxide and hydrogen rich gas
WO2018072888A1 (en) * 2016-10-20 2018-04-26 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of syngas
CN209840521U (en) * 2019-05-17 2019-12-24 成都赛普瑞兴科技有限公司 Equipment for separating and purifying carbon monoxide

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4805414A (en) * 1987-12-15 1989-02-21 Union Carbide Corporation Process to recover hydrogen-free higher boiling synthesis gas component
CN101627273A (en) * 2006-11-30 2010-01-13 林德股份公司 Method and device for obtaining products from synthesis gas
CN204006964U (en) * 2014-07-01 2014-12-10 开封空分集团有限公司 The device of Deep Cooling Method making pure carbon monoxide and hydrogen rich gas
WO2018072888A1 (en) * 2016-10-20 2018-04-26 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of syngas
CN209840521U (en) * 2019-05-17 2019-12-24 成都赛普瑞兴科技有限公司 Equipment for separating and purifying carbon monoxide

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112090106A (en) * 2020-09-15 2020-12-18 中国地质大学（武汉） Reagent purification device and method for purifying ammonium bifluoride or ammonium fluoride by using same

Also Published As

Publication number Publication date
CN110044133B (en) 2024-03-22

Similar Documents

Publication Publication Date Title
RU2331575C2 (en) Installation of cleaning with low δ p for the removal of nitrogen, methane and argon from syngas
KR100192874B1 (en) Air separation
CN106979664B (en) Atmospheric carbon dioxide liquifying method
TWI685468B (en) Method and apparatus for producing product nitrogen gas and product argon
CN104513680B (en) Technology and device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas
CN207335282U (en) Liquefaction lean gas removes heavy hydrocarbon system
CN108826831B (en) Device and process for cryogenic separation of carbon monoxide gas by nitrogen circulation refrigeration
RU2010150141A (en) IMPROVED NITROGEN REMOVAL IN A PLANT FOR PRODUCING LIQUEFIED NATURAL GAS
CN106288653A (en) A kind of single column cryogenic rectification reclaims device and the method for purification recovery argon of argon
RU2717668C1 (en) Low-temperature fractionation unit for complex gas treatment and production of lng
CN107367127A (en) A kind of cryogenic separation CO, H2Nitrogen cycle methane wash system and method
CN106461320A (en) Liquefied natural gas facility employing an optimized mixed refrigerant system
CN107062798A (en) Atmospheric carbon dioxide liquefaction system and method
US10317135B2 (en) Separation at sub-ambient temperature of a gaseous mixture containing carbon dioxide and a lighter contaminant
JP7451532B2 (en) Apparatus and method for separating air by cryogenic distillation
CN105135820B (en) LNG method and system is produced using gas containing air
CN203513622U (en) Device for removing hydrogen and nitrogen from methane-rich gas by rectifying and producing liquefied natural gas (LNG)
CN110044133A (en) The apparatus and method for of separating-purifying carbon monoxide
TW201800333A (en) Process and device for cryogenic synthesis gas separation
CN105066586B (en) Device for preparing raw material gas for synthetic ammonia and L NG by liquid nitrogen washing and preparation method thereof
US10899614B2 (en) Method and apparatus for producing a mixture of carbon monoxide and hydrogen
CN220070763U (en) Device for separating high-purity hydrogen chloride from byproduct hydrogen chloride of sucralose
CN114518016A (en) Carbon dioxide capturing, liquefying and recycling device and method
CN209840521U (en) Equipment for separating and purifying carbon monoxide
CN106979665B (en) Method and equipment for purifying synthetic gas

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant