CN202864908U - Coke-oven gas or LURGI furnace/British Gas-Lurgi furnace coal gasification ammonia-production co-production device - Google Patents

Coke-oven gas or LURGI furnace/British Gas-Lurgi furnace coal gasification ammonia-production co-production device Download PDF

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Publication number
CN202864908U
CN202864908U CN2012203434776U CN201220343477U CN202864908U CN 202864908 U CN202864908 U CN 202864908U CN 2012203434776 U CN2012203434776 U CN 2012203434776U CN 201220343477 U CN201220343477 U CN 201220343477U CN 202864908 U CN202864908 U CN 202864908U
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outlet
entrance
heat
interchanger
transfer lime
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章华勇
顾鹤燕
杨震东
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SHANGHAI INTERNATIONAL CONSTRUCTION ENGINEERING CONSULTING CO LTD
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SHANGHAI INTERNATIONAL CONSTRUCTION ENGINEERING CONSULTING CO LTD
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    • 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
    • F25J3/0233—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 CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0261—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon monoxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—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
    • F25J3/0276—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 H2/N2 mixtures, i.e. of ammonia 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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/80—Processes or apparatus using separation by rectification using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/14—Coke-ovens 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • 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
    • F25J2215/02—Mixing or blending of fluids to yield a certain product
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
    • 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
    • F25J2270/14—External refrigeration with work-producing gas expansion 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

The utility model discloses a coke-oven gas or LURGI furnace/British Gas-Lurgi furnace coal gasification ammonia-production co-production device which comprises a first heat exchange, a second heat exchanger, a third heat exchanger and an ammonia washing tower and is characterized by further comprising a methane rectifying tower, a condenser at the top of the methane rectifying tower, a reboiler at the bottom of the methane rectifying tower, a feed gas flash tank, a CO liquid enriching tank and a liquid methane pump which are connected by pipelines. According to the utility model, the methane rectifying tower and the liquid methane pump are additionally arranged in a conventional liquid nitrogen washing device; the methane-enriched fractions are reheated and then output as city gas through reasonable line configuration; the methane-enriched fractions can be also subjected to Claude circular cooling to product an LNG (Liquefied Natural Gas) product; and meanwhile, an SNG (Synthetic Natural Gas) and the LNG can be subjected to product adjustment according to different using loads.

Description

Coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed
Technical field
The utility model relates to coke(oven)gas or LURGI stove/BGL stove and produces synthetic ammonia technical gas field of purification in the coal chemical technology of synthetic ammonia, be particularly related to a kind of take coal as raw material, utilize LURGI stove or BGL stove to be the gasification mode, or the raw hydrogen take coke(oven)gas as raw material (hydrogen, carbon monoxide, nitrogen, methane, argon), purify the preparation ammonia synthetic fresh gas, produce synthetic ammonia, and coproduction SNG is or/and the device of LNG and high-pressure gas product.The utility model mainly is exactly for adopting coke(oven)gas or LURGI stove/BGL stove to produce the coal chemical technology of synthetic ammonia.
Background technology
Because the deficiency of petroleum and natural gas reserves, domestic a large amount of Development of Coal chemical industry, it is whether suitable that gasification is selected is exactly key, however coal is depended in the selection of gasification, the final raw gas specification of different coals, different coal generating gas is far from each other.In addition, in line with the principle that coke(oven)gas in the coking industry is rationally taken full advantage of, coke(oven)gas also is used for chemical industry in a large number.
As everyone knows, in the raw gas of coke(oven)gas or LURGI stove/BGL outlet of still, basal component also has part methane, argon except carbon monoxide, hydrogen, in the synthetic ammonia process of producing product, need to remove through the liquid nitrogen washing operation gases harmful to catalyzer such as the rare gas element such as methane and carbon monoxide, could satisfy the requirement that synthetic ammonia process is produced.For the methane rich cut that separates, domestic each coal chemical industry enterprises is taked different processing modes.
One, referring to Fig. 1, raw gas/coke(oven)gas is removed the rare gas element such as methane and carbon monoxide etc. and is delivered to synthetic ammonia process after to the harmful gas of catalyzer through delivering to low-temperature rectisol, liquid nitrogen washing operation after the CO conversion, and Zhongdao synthesis procedure is produced ammonia.The low-temperature rectisol operation is got back to again after directly delivering to methane conversion, non-sulfur-resisting transformation workshop section after with the methane rich cut re-heat out of liquid nitrogen washing operation by some enterprises.
The method exists following obvious deficiency: 1, flow process is oversize, is unfavorable for device steady running and management; 2, product structure simplification, added value is low; 3, methane concentration and the rate of recovery low; 4, investment is high, and cost performance is low.
Its two, for some New Coal Chemical devices, referring to Fig. 2, increased that liquid nitrogen washing purifies and by-product SNG.
For this technique because the difference of flow process configuration, adopt at present or applied for a patent all have a following deficiency: 1, methane rich concentration is lower, and calorific value is lower, does not meet the requirement of town gas product specification; 2, the methane rich product recovery rate is low, causes energy dissipation; 3, owing to the unreasonable waste that causes the low temperature cold of flow process configuration, energy consumption is higher; 4, the SNG gas product that by-product is single can't be adjusted the product mix when having the different demand of town gas.
SNG/LNG is the clean energy that develops rapidly in recent years, has the characteristics pollution-free, that calorific value is high, and SNG can be directly as town gas; But, no matter be the variation in season or the difference of time, all there is the peak valley section of usefulness gas in town gas, considers the difficulty of town gas accumulating, produces simultaneously the LNG natural gas liquids to adjust the product mix, and reply is moving with wave to be imperative.
From present development, for coke(oven)gas or LURGI stove/BGL furnace gas metallization processes, also there are many patents to mention synthetic ammonia and SNG joint process, but because the difference of flow process configuration, the type selecting of product structure, product specification, energy consumption and equipment has larger difference, and while by-product SNG and LNG not yet have patent to mention, so the key problem of this patent is to realize gas cleaning and the higher product of production added value such as how lower energy consumption.
The utility model content
One of technical problem to be solved in the utility model is to wash the existing problem of technique and coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed are provided for low temperature liquid nitrogen in existing coke(oven)gas or LURGI stove/BGL furnace gas and the production ammonia synthesis process, this device is washed workshop section by low temperature liquid nitrogen and is removed CO, Ar, the impurity such as CH4 and rare gas element purify ammonia synthetic fresh gas, regulate hydrogen nitrogen ratio to satisfy ammonia synthesis process to the requirement of virgin gas, by to methane rectifying tower reasonable disposition on stream, realize that under the condition of less energy-consumption the production of high yield meets the SNG of relevant criterion.
Two of technical problem to be solved in the utility model is to wash the existing problem of technique and coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed are provided for low temperature liquid nitrogen in existing coke(oven)gas or the LURGI stove/BGL furnace gas production ammonia synthesis process, this device is washed workshop section by low temperature liquid nitrogen and is removed CO, Ar, the impurity such as CH4 and rare gas element purify ammonia synthetic fresh gas, regulate hydrogen nitrogen ratio to satisfy ammonia synthesis process to the requirement of virgin gas, by to methane rectifying tower reasonable disposition on stream, realize that under the condition of less energy-consumption the production of high yield meets LNG and the high-pressure gas of relevant criterion.
Three of technical problem to be solved in the utility model is to wash the existing problem of technique and coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed are provided for low temperature liquid nitrogen in existing coke(oven)gas or the LURGI stove/BGL furnace gas production ammonia synthesis process, this device is washed workshop section by low temperature liquid nitrogen and is removed CO, Ar, the impurity such as CH4 and rare gas element are prepared ammonia synthetic fresh gas, regulate hydrogen nitrogen ratio to satisfy ammonia synthesis process to the requirement of virgin gas, by to methane rectifying tower reasonable disposition on stream, realize that under the condition of less energy-consumption the production of high yield meets the SNG of relevant criterion, LNG and high-pressure gas.Can regulate the SNG/LNG product structure by operation simultaneously, to solve downstream user in the impact of Various Seasonal demands different from the period on the fluctuation generation, realize the steady running of whole synthetic ammonia installation.
Coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed as the utility model first aspect, comprise First Heat Exchanger, the second interchanger, the 3rd interchanger and nitrogen wash column, it is characterized in that, also comprise methane rectifying tower, methane rectifying tower cat head condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, carbon monoxide rich solution tank, liquid methane pump;
Divide the first high pressure nitrogen transfer lime that is connected to be connected with the first condensation entrance of described First Heat Exchanger with sky, one end of the second high pressure nitrogen transfer lime is connected with the first condensation of described First Heat Exchanger outlet, the first condensation entrance is communicated with the first condensation outlet, the other end of the second high pressure nitrogen transfer lime is connected with the second condensation entrance of described the second interchanger, third high presses an end of nitrogen transfer lime to be connected with the second condensation outlet of described the second interchanger, the second condensation entrance is communicated with the second condensation outlet, third high presses the other end of nitrogen transfer lime to be divided into two strands, and one third high presses the nitrogen transfer lime to be connected with the 3rd condensation entrance of described the 3rd interchanger; The 3rd condensation outlet of described the 3rd interchanger connects an end of the first high pressure low temperature liquid nitrogen transfer lime, and the 3rd condensation entrance is communicated with the 3rd condensation outlet, and the first high pressure low temperature liquid nitrogen transfer lime is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top;
The the first raw hydrogen transfer lime that is connected with molecular sieve is connected with the 4th condensation entrance of described the second interchanger, one end of the second raw hydrogen transfer lime is connected with the 4th condensation of described the second interchanger outlet, the 4th condensation entrance is communicated with the 4th condensation outlet, the other end of the second raw hydrogen transfer lime is connected with the 5th condensation entrance of described the 3rd interchanger, one end of the 3rd raw hydrogen transfer lime is connected with the 5th condensation of described the 3rd interchanger outlet, the 5th condensation entrance is communicated with the 5th condensation outlet, and the other end of the 3rd raw hydrogen transfer lime is connected with the raw hydrogen entrance on described unstripped gas flash tank top;
Described unstripped gas flash tank cat head is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of the unstripped gas flash tank tower, the first gaseous phase outlet is connected with the first gas phase entrance of nitrogen wash column bottom by the first gas-phase transport pipe, and the first liquid-phase outlet is connected with the second liquid phase entrance of methane rectifier by the first liquid phase transfer lime;
Be provided with at the top of nitrogen wash column and remove CO, Ar, CH 4The second gaseous phase outlet behind the impurity, the bottom of nitrogen wash column is provided with liquid rich CO cut outlet, the second gaseous phase outlet connects by the 3rd re-heat entrance of the second gas-phase transport Guan Yudi three interchanger, the 3rd re-heat outlet of the 3rd interchanger is communicated with the 3rd re-heat entrance, the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe, and the second gas-phase transport pipe presses the nitrogen transfer lime to be connected with another burst third high; The 4th re-heat outlet of the second interchanger is the first virgin gas transfer lime, the first virgin gas transfer lime is divided into two strands, wherein the other end of one the first virgin gas transfer lime is connected with the entrance of described methane rectifying tower tower bottom reboiler, the outlet of methane rectifying tower tower bottom reboiler connects low-temperature rectisol workshop section entrance by the second virgin gas transfer lime, and the re-heat outlet of low-temperature rectisol workshop section connects the 3rd virgin gas transfer lime; The other end of another strand the first virgin gas transfer lime connects the 6th re-heat entrance of First Heat Exchanger, and the 6th re-heat outlet of First Heat Exchanger connects ammonia synthesis workshop section by the bright letter shoot of the "four news" (new ideas, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Described the 3rd virgin gas transfer lime is connected the rear ammonia synthetic fresh gas that forms with the bright letter shoot of the described "four news" (new ideas;
The liquid rich CO cut outlet of nitrogen wash column bottom is connected to the entrance of carbon monoxide rich solution tank by the rich CO cut of liquid state transfer lime, the top of carbon monoxide rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of carbon monoxide rich solution tank is provided with the 3rd liquid-phase outlet; The 3rd liquid-phase outlet is connected with the cold junction entrance of methane rectifying tower cat head condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower cat head condenser connects an end of the 5th gas-phase transport pipe, the 4th gaseous phase outlet connects an end of the 4th gas-phase transport pipe, the other end of the other end of the 4th gas-phase transport pipe and the 5th gas-phase transport pipe and connect after the 7th re-heat entrance by the 6th gas-phase transport Guan Yudi three interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat of the 3rd interchanger outlet, and the 7th re-heat entrance is communicated with the 7th re-heat outlet; The other end of the first exhaust pipe is connected with the 8th re-heat entrance of the second interchanger, one end of the second exhaust pipe is connected with the 8th re-heat of the second interchanger outlet, the 8th re-heat outlet is communicated with the 8th re-heat entrance, the other end of the second exhaust pipe is connected with the 9th re-heat entrance of First Heat Exchanger, one end of the 3rd exhaust pipe is connected with the 9th re-heat of First Heat Exchanger outlet, the 9th re-heat outlet is communicated with another termination gas ductwork of the 3rd exhaust pipe with the 9th re-heat entrance;
The top of described methane rectifying tower is provided with the 3rd gaseous phase outlet, the bottom of methane rectifying tower is provided with the outlet of methane rich liquid phase, the 3rd gaseous phase outlet is connected with the hot junction entrance of described methane rectifying tower cat head condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower cat head condenser is connected with the 4th liquid phase transfer lime;
The methane rich liquid phase outlet of methane rectifier bottoms connects the tenth re-heat entrance of the second interchanger by the first methane rich liquid phase transfer lime, one end of the second methane rich liquid phase transfer lime is connected to the tenth re-heat outlet of the second interchanger, the tenth re-heat outlet is communicated with the tenth re-heat entrance, the other end of the second methane rich liquid phase transfer lime is connected to the 11 re-heat entrance of First Heat Exchanger, the 11 re-heat outlet of First Heat Exchanger is connected to the SNG storage tank by the SNG line of pipes, and the 11 re-heat outlet is communicated with the 11 re-heat entrance;
The methane rich liquid phase outlet of described methane rectifier bottoms also is connected with one the 3rd methane rich liquid phase transfer lime, the 3rd methane rich liquid phase transfer lime is connected with the entrance of described liquid methane pump, described liquid methane pump outlet is connected to the 12 re-heat entrance of the second interchanger by the 4th methane rich liquid phase transfer lime, the 12 re-heat outlet of the second interchanger is connected to the 13 re-heat entrance of First Heat Exchanger by the 5th methane rich liquid phase transfer lime, the 12 re-heat outlet is communicated with the 12 re-heat entrance, and the 13 re-heat outlet of First Heat Exchanger is connected to gasification workshop section by the high-pressure gas transfer lime; The 13 re-heat outlet is communicated with the 13 re-heat entrance.
In coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, described methane rectifying tower cat head condenser is built in the described methane rectifying tower, and the 3rd gaseous phase outlet at described methane rectifying tower top connects with the hot junction outlet of methane rectifying tower cat head condenser.
In coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, also comprise a methane rectifying tower return tank, described methane rectifying tower cat head condenser is external outside methane rectifying tower cat head, and the hot junction outlet of described methane rectifying tower cat head condenser is connected with the entrance of methane rectifying tower return tank; Top at methane rectifying tower return tank is provided with the 7th gaseous phase outlet, and the bottom of methane rectifying tower return tank is provided with bypass outlet; Top at the methane rectifying tower is provided with reflux inlet, and the 7th gaseous phase outlet is connected with described the first exhaust pipe by the 7th gas-phase transport pipe; The bypass outlet of methane rectifying tower return tank bottom is connected by the reflux inlet of return line with the methane rectifier.
Be provided with liquid nitrogen in the bottom of described C0 rich solution tank and replenish mouth, this liquid nitrogen replenishes mouth and replenishes pipe connecting fluid nitrogenous source by liquid nitrogen.
Described third high presses the other end of nitrogen transfer lime not tell two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime are told in the 3rd condensation outlet of described the 3rd interchanger, be connected to the first re-heat entrance of described the 3rd interchanger on the first high pressure low temperature liquid nitrogen transfer lime the other end behind series connection one reducing valve, the second high pressure low temperature liquid nitrogen transfer lime the other end is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top; The first liquid-phase outlet is connected with the second re-heat entrance of described the 3rd interchanger by the first liquid phase transfer lime, the second re-heat outlet of the 3rd interchanger is connected with the second liquid phase entrance of methane rectifier by the second liquid phase transfer lime, and the second re-heat entrance is communicated with the second re-heat outlet; The 3rd re-heat outlet of the 3rd interchanger is communicated with the first re-heat entrance and the 3rd re-heat entrance, and the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe.
Coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed as the utility model second aspect, comprise First Heat Exchanger, the second interchanger, the 3rd interchanger and nitrogen wash column, it is characterized in that, also comprise methane rectifying tower, methane rectifying tower cat head condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, carbon monoxide rich solution tank, liquid methane pump;
Divide the first high pressure nitrogen transfer lime that is connected to be connected with the first condensation entrance of described First Heat Exchanger with sky, one end of the second high pressure nitrogen transfer lime is connected with the first condensation of described First Heat Exchanger outlet, the first condensation entrance is communicated with the first condensation outlet, the other end of the second high pressure nitrogen transfer lime is connected with the second condensation entrance of described the second interchanger, third high presses an end of nitrogen transfer lime to be connected with the second condensation outlet of described the second interchanger, the second condensation entrance is communicated with the second condensation outlet, third high presses the other end of nitrogen transfer lime to be divided into two strands, and one third high presses the nitrogen transfer lime to be connected with the 3rd condensation entrance of described the 3rd interchanger; The 3rd condensation outlet of described the 3rd interchanger connects an end of the first high pressure low temperature liquid nitrogen transfer lime, and the 3rd condensation entrance is communicated with the 3rd condensation outlet, and the first high pressure low temperature liquid nitrogen transfer lime is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top;
The the first raw hydrogen transfer lime that is connected with molecular sieve is connected with the 4th condensation entrance of described the second interchanger, one end of the second raw hydrogen transfer lime is connected with the 4th condensation of described the second interchanger outlet, the 4th condensation entrance is communicated with the 4th condensation outlet, the other end of the second raw hydrogen transfer lime is connected with the 5th condensation entrance of described the 3rd interchanger, one end of the 3rd raw hydrogen transfer lime is connected with the 5th condensation of described the 3rd interchanger outlet, the 5th condensation entrance is communicated with the 5th condensation outlet, and the other end of the 3rd raw hydrogen transfer lime is connected with the raw hydrogen entrance on described unstripped gas flash tank top;
Described unstripped gas flash tank cat head is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of the unstripped gas flash tank tower, the first gaseous phase outlet is connected with the first gas phase entrance of nitrogen wash column bottom by the first gas-phase transport pipe, and the first liquid-phase outlet is connected with the second liquid phase entrance of methane rectifier by the first liquid phase transfer lime;
Be provided with at the top of nitrogen wash column and remove CO, Ar, CH 4The second gaseous phase outlet behind the impurity, the bottom of nitrogen wash column is provided with liquid rich CO cut outlet, the second gaseous phase outlet connects by the 3rd re-heat entrance of the second gas-phase transport Guan Yudi three interchanger, the 3rd re-heat outlet of the 3rd interchanger is communicated with the first re-heat entrance and the 3rd re-heat entrance, the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe, and the second gas-phase transport pipe presses the nitrogen transfer lime to be connected with another burst third high; The 4th re-heat outlet of the second interchanger is the first virgin gas transfer lime, the first virgin gas transfer lime is divided into two strands, wherein the other end of one the first virgin gas transfer lime is connected with the entrance of described methane rectifying tower tower bottom reboiler, the outlet of methane rectifying tower tower bottom reboiler connects low-temperature rectisol workshop section entrance by the second virgin gas transfer lime, and the re-heat outlet of low-temperature rectisol workshop section connects the 3rd virgin gas transfer lime; The other end of another strand the first virgin gas transfer lime connects the 6th re-heat entrance of First Heat Exchanger, and the 6th re-heat outlet of First Heat Exchanger connects ammonia synthesis workshop section by the bright letter shoot of the "four news" (new ideas, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Described the 3rd virgin gas transfer lime is connected with the bright letter shoot of the described "four news" (new ideas;
The liquid rich CO cut outlet of nitrogen wash column bottom is connected to the entrance of carbon monoxide rich solution tank by the rich CO cut of liquid state transfer lime, the top of carbon monoxide rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of carbon monoxide rich solution tank is provided with the 3rd liquid-phase outlet; The 3rd liquid-phase outlet is connected with the cold junction entrance of methane rectifying tower cat head condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower cat head condenser connects an end of the 5th gas-phase transport pipe, the 4th gaseous phase outlet connects an end of the 4th gas-phase transport pipe, the other end of the other end of the 4th gas-phase transport pipe and the 5th gas-phase transport pipe and connect after the 7th re-heat entrance by the 6th gas-phase transport Guan Yudi three interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat of the 3rd interchanger outlet, and the 7th re-heat entrance is communicated with the 7th re-heat outlet; The other end of the first exhaust pipe is connected with the 8th re-heat entrance of the second interchanger, one end of the second exhaust pipe is connected with the 8th re-heat of the second interchanger outlet, the 8th re-heat outlet is communicated with the 8th re-heat entrance, the other end of the second exhaust pipe is connected with the 9th re-heat entrance of First Heat Exchanger, one end of the 3rd exhaust pipe is connected with the 9th re-heat of First Heat Exchanger outlet, the 9th re-heat outlet is communicated with another termination gas ductwork of the 3rd exhaust pipe with the 9th re-heat entrance;
The top of described methane rectifying tower is provided with the 3rd gaseous phase outlet, the bottom of methane rectifying tower is provided with the outlet of methane rich liquid phase, the 3rd gaseous phase outlet is connected with the hot junction entrance of described methane rectifying tower cat head condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower cat head condenser is connected with the 4th liquid phase transfer lime;
The methane rich liquid phase outlet of methane rectifier bottoms is connected to the entrance of liquid methane pump by the 6th methane rich liquid phase transfer lime, the liquid methane pump outlet connects the 7th methane rich liquid phase transfer lime and the 8th methane rich liquid phase transfer lime, be provided with variable valve at the 7th methane rich liquid phase transfer lime and the 8th methane rich liquid phase transfer lime, the other end of the 7th methane rich liquid phase transfer lime is connected with the 14 condensation entrance of the 3rd interchanger, and the 14 condensation outlet of the 3rd interchanger connects the LNG storage tank by the LNG transfer lime; The 8th methane rich liquid phase transfer lime is connected with the 12 re-heat entrance of the second interchanger, the 12 re-heat outlet of the second interchanger is connected to the 13 re-heat entrance of First Heat Exchanger by the 5th methane rich liquid phase transfer lime, the 12 re-heat outlet is communicated with the 12 re-heat entrance, and the 13 re-heat outlet of First Heat Exchanger is connected to gasification workshop section by the high-pressure gas transfer lime; The 13 re-heat outlet is communicated with the 13 re-heat entrance.
In coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, described methane rectifying tower cat head condenser is built in the described methane rectifying tower, and the 3rd gaseous phase outlet at described methane rectifying tower top connects with the hot junction outlet of methane rectifying tower cat head condenser.
In coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, also comprise a methane rectifying tower return tank, described methane rectifying tower cat head condenser is external outside methane rectifying tower cat head, and the hot junction outlet of described methane rectifying tower cat head condenser is connected with the entrance of methane rectifying tower return tank; Top at methane rectifying tower return tank is provided with the 7th gaseous phase outlet, and the bottom of methane rectifying tower return tank is provided with bypass outlet; Top at the methane rectifying tower is provided with reflux inlet, and the 7th gaseous phase outlet is connected with described the first exhaust pipe by the 7th gas-phase transport pipe; The bypass outlet of methane rectifying tower return tank bottom is connected by the reflux inlet of return line with the methane rectifier.
In coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, between described First Heat Exchanger and the second interchanger, connect a Claude cycle refrigeration system; This Claude cycle refrigeration system is by a decompressor, one compressor and a water cooler form, wherein the entrance of compressor is connected with the first cold loop exit of First Heat Exchanger, the outlet of compressor is connected with the hot junction entrance of water cooler, the hot junction outlet of water cooler is connected with the second cold loop head of First Heat Exchanger, the second cold loop exit of First Heat Exchanger is connected with the 3rd cold loop head of the second interchanger, the second cold loop exit is communicated with the second cold loop head, the 3rd cold loop exit of the second interchanger is connected with the entrance of decompressor, the outlet of decompressor is connected with the 4th cold loop head of the second interchanger, the 4th cold loop exit of the second interchanger is connected with the first cold loop head of First Heat Exchanger, the 4th cold loop exit is communicated with the 4th cold loop head, and the first cold loop head is communicated with the first cold loop exit.
Described third high presses the other end of nitrogen transfer lime not tell two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime are told in the 3rd condensation outlet of described the 3rd interchanger, be connected to the first re-heat entrance of described the 3rd interchanger on the first high pressure low temperature liquid nitrogen transfer lime the other end behind series connection one reducing valve, the second high pressure low temperature liquid nitrogen transfer lime the other end is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top; The first liquid-phase outlet is connected with the second re-heat entrance of described the 3rd interchanger by the first liquid phase transfer lime, the second re-heat outlet of the 3rd interchanger is connected with the second liquid phase entrance of methane rectifier by the second liquid phase transfer lime, and the second re-heat entrance is communicated with the second re-heat outlet; The 3rd re-heat outlet of the 3rd interchanger is communicated with the first re-heat entrance and the 3rd re-heat entrance, and the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe.
Coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed as the utility model third aspect, comprise First Heat Exchanger, the second interchanger, the 3rd interchanger and nitrogen wash column, it is characterized in that, also comprise methane rectifying tower, methane rectifying tower cat head condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, carbon monoxide rich solution tank;
Divide the first high pressure nitrogen transfer lime that is connected to be connected with the first condensation entrance of described First Heat Exchanger with sky, one end of the second high pressure nitrogen transfer lime is connected with the first condensation of described First Heat Exchanger outlet, the first condensation entrance is communicated with the first condensation outlet, the other end of the second high pressure nitrogen transfer lime is connected with the second condensation entrance of described the second interchanger, third high presses an end of nitrogen transfer lime to be connected with the second condensation outlet of described the second interchanger, the second condensation entrance is communicated with the second condensation outlet, third high presses the other end of nitrogen transfer lime to be divided into two strands, and one third high presses the nitrogen transfer lime to be connected with the 3rd condensation entrance of described the 3rd interchanger; The 3rd condensation outlet of described the 3rd interchanger connects an end of the first high pressure low temperature liquid nitrogen transfer lime, and the 3rd condensation entrance is communicated with the 3rd condensation outlet, and the first high pressure low temperature liquid nitrogen transfer lime is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top;
The the first raw hydrogen transfer lime that is connected with molecular sieve is connected with the 4th condensation entrance of described the second interchanger, one end of the second raw hydrogen transfer lime is connected with the 4th condensation of described the second interchanger outlet, the 4th condensation entrance is communicated with the 4th condensation outlet, the other end of the second raw hydrogen transfer lime is connected with the 5th condensation entrance of described the 3rd interchanger, one end of the 3rd raw hydrogen transfer lime is connected with the 5th condensation of described the 3rd interchanger outlet, the 5th condensation entrance is communicated with the 5th condensation outlet, and the other end of the 3rd raw hydrogen transfer lime is connected with the raw hydrogen entrance on described unstripped gas flash tank top;
Described unstripped gas flash tank cat head is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of the unstripped gas flash tank tower, the first gaseous phase outlet is connected with the first gas phase entrance of nitrogen wash column bottom by the first gas-phase transport pipe, and the first liquid-phase outlet is connected with the second liquid phase entrance of methane rectifier by the first liquid phase transfer lime;
Be provided with at the top of nitrogen wash column and remove CO, Ar, CH 4The second gaseous phase outlet behind the impurity, the bottom of nitrogen wash column is provided with liquid rich CO cut outlet, the second gaseous phase outlet connects by the 3rd re-heat entrance of the second gas-phase transport Guan Yudi three interchanger, the 3rd re-heat outlet of the 3rd interchanger is communicated with the first re-heat entrance and the 3rd re-heat entrance, the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe, and the second gas-phase transport pipe presses the nitrogen transfer lime to be connected with another burst third high; The 4th re-heat outlet of the second interchanger is the first virgin gas transfer lime, the first virgin gas transfer lime is divided into two strands, wherein the other end of one the first virgin gas transfer lime is connected with the entrance of described methane rectifying tower tower bottom reboiler, the outlet of methane rectifying tower tower bottom reboiler connects low-temperature rectisol workshop section entrance by the second virgin gas transfer lime, and the re-heat outlet of low-temperature rectisol workshop section connects the 3rd virgin gas transfer lime; The other end of another strand the first virgin gas transfer lime connects the 6th re-heat entrance of First Heat Exchanger, and the 6th re-heat outlet of First Heat Exchanger connects ammonia synthesis workshop section by the bright letter shoot of the "four news" (new ideas, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Described the 3rd virgin gas transfer lime is connected with the bright letter shoot of the described "four news" (new ideas;
The liquid rich CO cut outlet of nitrogen wash column bottom is connected to the entrance of carbon monoxide rich solution tank by the rich CO cut of liquid state transfer lime, the top of carbon monoxide rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of carbon monoxide rich solution tank is provided with the 3rd liquid-phase outlet; The 3rd liquid-phase outlet is connected with the cold junction entrance of methane rectifying tower cat head condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower cat head condenser connects an end of the 5th gas-phase transport pipe, the 4th gaseous phase outlet connects an end of the 4th gas-phase transport pipe, the other end of the other end of the 4th gas-phase transport pipe and the 5th gas-phase transport pipe and connect after the 7th re-heat entrance by the 6th gas-phase transport Guan Yudi three interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat of the 3rd interchanger outlet, and the 7th re-heat entrance is communicated with the 7th re-heat outlet; The other end of the first exhaust pipe is connected with the 8th re-heat entrance of the second interchanger, one end of the second exhaust pipe is connected with the 8th re-heat of the second interchanger outlet, the 8th re-heat outlet is communicated with the 8th re-heat entrance, the other end of the second exhaust pipe is connected with the 9th re-heat entrance of First Heat Exchanger, one end of the 3rd exhaust pipe is connected with the 9th re-heat of First Heat Exchanger outlet, the 9th re-heat outlet is communicated with another termination gas ductwork of the 3rd exhaust pipe with the 9th re-heat entrance;
The top of described methane rectifying tower is provided with the 3rd gaseous phase outlet, the bottom of methane rectifying tower is provided with the outlet of methane rich liquid phase, the 3rd gaseous phase outlet is connected with the hot junction entrance of described methane rectifying tower cat head condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower cat head condenser is connected with the 4th liquid phase transfer lime;
The methane rich liquid phase outlet of methane rectifier bottoms also is connected to the first methane rich liquid phase transfer lime and the tenth methane rich liquid phase transfer lime, be provided with variable valve at the first methane rich liquid phase transfer lime, the other end of the first methane rich liquid phase transfer lime is connected with the tenth re-heat entrance of the second interchanger, one end of the second methane rich liquid phase transfer lime is connected to the tenth re-heat outlet of the second interchanger, the tenth re-heat outlet is communicated with the tenth re-heat entrance, the other end of the second methane rich liquid phase transfer lime is connected to the 11 re-heat entrance of First Heat Exchanger, the 11 re-heat outlet of First Heat Exchanger is connected to the SNG storage tank by the SNG line of pipes, and the 11 re-heat outlet is communicated with the 11 re-heat entrance; The tenth methane rich liquid phase transfer lime is connected to the entrance of liquid methane pump, the liquid methane pump outlet also connects the 7th methane rich liquid phase transfer lime and the 8th methane rich liquid phase transfer lime, be provided with variable valve at the 7th methane rich liquid phase transfer lime and the 8th methane rich liquid phase transfer lime, the other end of the 7th methane rich liquid phase transfer lime is connected with the 14 re-heat entrance of the 3rd interchanger, and the 14 re-heat outlet of the 3rd interchanger connects the LNG storage tank by the LNG transfer lime; The 8th methane rich liquid phase transfer lime is connected with the 12 re-heat entrance of the second interchanger, the 12 re-heat outlet of the second interchanger is connected to the 13 re-heat entrance of First Heat Exchanger by the 5th methane rich liquid phase transfer lime, the 12 re-heat outlet is communicated with the 12 re-heat entrance, and the 13 re-heat outlet of First Heat Exchanger is connected to gasification workshop section by the high-pressure gas transfer lime; The 13 re-heat outlet is communicated with the 13 re-heat entrance.
In coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, described methane rectifying tower cat head condenser is built in the described methane rectifying tower, and the 3rd gaseous phase outlet at described methane rectifying tower top connects with the hot junction outlet of methane rectifying tower cat head condenser.
In coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, also comprise a methane rectifying tower return tank, described methane rectifying tower cat head condenser is external outside methane rectifying tower cat head, and the hot junction outlet of described methane rectifying tower cat head condenser is connected with the entrance of methane rectifying tower return tank; Top at methane rectifying tower return tank is provided with the 7th gaseous phase outlet, and the bottom of methane rectifying tower return tank is provided with bypass outlet; Top at the methane rectifying tower is provided with reflux inlet, and the 7th gaseous phase outlet is connected with described the first exhaust pipe by the 7th gas-phase transport pipe; The bypass outlet of methane rectifying tower return tank bottom is connected by the reflux inlet of return line with the methane rectifier.
In coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, between described First Heat Exchanger and the second interchanger, connect a Claude cycle refrigeration system; This Claude cycle refrigeration system is by a decompressor, one compressor and a water cooler form, wherein the entrance of compressor is connected with the first cold loop exit of First Heat Exchanger, the outlet of the first decompressor is connected with the hot junction entrance of water cooler, the hot junction outlet of water cooler is connected with the second cold loop head of First Heat Exchanger, the second cold loop exit of First Heat Exchanger is connected with the 3rd cold loop head of the second interchanger, the second cold loop exit is communicated with the second cold loop head, the 3rd cold loop exit of the second interchanger is connected with the entrance of the second decompressor, the outlet of the second decompressor is connected with the 4th cold loop head of the second interchanger, the 4th cold loop exit of the second interchanger is connected with the first cold loop head of First Heat Exchanger, the 4th cold loop exit is communicated with the 4th cold loop head, and the first cold loop head is communicated with the first cold loop exit.
In above-mentioned coke(oven)gas or the LURGI stove/BGL producer gas ammonia combination preparing device processed, be provided with liquid nitrogen in the bottom of described carbon monoxide rich solution tank and replenish mouth, this liquid nitrogen replenishes mouth and replenishes pipe connecting fluid nitrogenous source by liquid nitrogen.
Described third high presses the other end of nitrogen transfer lime not tell two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime are told in the 3rd condensation outlet of described the 3rd interchanger, be connected to the first re-heat entrance of described the 3rd interchanger on the first high pressure low temperature liquid nitrogen transfer lime the other end behind series connection one reducing valve, the second high pressure low temperature liquid nitrogen transfer lime the other end is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top; The first liquid-phase outlet is connected with the second re-heat entrance of described the 3rd interchanger by the first liquid phase transfer lime, the second re-heat outlet of the 3rd interchanger is connected with the second liquid phase entrance of methane rectifier by the second liquid phase transfer lime, and the second re-heat entrance is communicated with the second re-heat outlet; The 3rd re-heat outlet of the 3rd interchanger is communicated with the first re-heat entrance and the 3rd re-heat entrance, and the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe.
Owing to having adopted technical scheme as above, the utility model arranges methane rectifying tower, methane rectifying tower cat head condenser, methane rectifying column top return tank, methane rectifying tower tower bottom reboiler, liquid methane pump in the middle of the second and the 3rd interchanger, to reach the purpose of coproduction SNG and LNG and high-pressure gas.
Utilize the purpose of low temperature cold in order to reach maximum, return after the liquid phase constant enthalpy decompression from the unstripped gas flash tank and enter into the methane rectifying tower after the 3rd interchanger reclaims cold, can greatly lower like this consumption of low temperature cold, namely reduce energy consumption.
Methane rectifying tower of the present utility model adopts the operating method of total reflux, control the quality of methane product at the bottom of the methane rectifying tower by quantity of reflux, the cold of methane rectifying tower cat head condenser comes from the liquid phase of carbon monoxide rich solution tank, and methane rectifying tower tower bottom reboiler thermal source is from the part virgin gas logistics of going to low-temperature rectisol workshop section; Adopt this mode can reclaim to greatest extent methane in the unstripped gas, reach simultaneously the purpose of product concentrate, make product satisfy national standard.
Methane rectifying tower cat head condenser of the present utility model, tower bottom reboiler are loaded adjustable, to adapt to different operating modes and to satisfy the finished product requirement.
Thereby methane rectifying tower cat head condenser of the present utility model can be built directly into cancellation methane rectifying column top return tank in the methane rectifying tower, reduces facility investment.
The utility model utilizes LURGI stove or BGL stove to be the gasification mode for coke(oven)gas or take coal as raw material, purifies raw hydrogen, preparation ammonia synthetic fresh gas, final production synthetic ammonia, and the product of by-product SNG Sweet natural gas specification and LNG natural gas liquids specification.Be applicable to less energy-consumption new type low temperature liquid nitrogen washing (gas removal) the coproduction SNG/LNG technology that raw hydrogen (hydrogen, carbon monoxide, nitrogen, methane, argon) purifies synthetic ammonia processed field.
Description of drawings
Fig. 1 removes the rare gas element such as methane and carbon monoxide etc. and delivers to synthetic ammonia process after to the harmful gas of catalyzer through delivering to low-temperature rectisol, liquid nitrogen washing operation after the CO conversion for existing raw gas/coke(oven)gas, and Zhongdao synthesis procedure is produced the schema of ammonia process.
Fig. 2 purifies the also process flow sheet of by-product SNG for increasing liquid nitrogen washing.
Fig. 3 is the process flow sheet that the utility model coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purify preparation ammonia synthetic fresh gas and coproduction SNG and/or LNG.
Fig. 4 is a kind of device schema that the utility model coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purify preparation ammonia synthetic fresh gas and coproduction SNG.
Fig. 5 is the another kind of device schema that the utility model coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purify preparation ammonia synthetic fresh gas and coproduction SNG.
Fig. 6 is a kind of device schema that the utility model coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purify preparation ammonia synthetic fresh gas and coproduction LNG.
Fig. 7 is the another kind of device schema that the utility model coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purify preparation ammonia synthetic fresh gas and coproduction LNG.
Fig. 8 is a kind of device schema that the utility model coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purify preparation ammonia synthetic fresh gas and coproduction SNG and LNG.
Fig. 9 is the another kind of device schema that the utility model coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purify preparation ammonia synthetic fresh gas and coproduction SNG and LNG.Figure 10 is that the utility model methane rectifying tower cat head condenser is built in the structural representation in the described methane rectifying tower.
Embodiment
Referring to Fig. 3, technical process of the present utility model is that raw gas/coke(oven)gas is through CO conversion, low-temperature rectisol, liquid nitrogen washing synthetic virgin gas coproduction SNG, LNG and high-pressure gas.Specific embodiment is as follows:
Embodiment 1
Referring to Fig. 4, Fig. 4 has provided coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies a kind of device schema of preparing ammonia synthetic fresh gas and coproduction SNG.
This coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies the device of preparation ammonia synthetic fresh gas coproduction SNG and high-pressure gas, comprises interchanger 100,200,300, nitrogen wash column 400, methane rectifying tower 500, methane rectifying tower cat head condenser 600, methane rectifying tower tower bottom reboiler 700, unstripped gas flash tank 800, C0 rich solution tank 900, liquid methane pump 1000, methane rectifying tower return tank 1500.
Divide the nitrogen compressor 1100 that is connected to be connected with the condensation entrance 120 of interchanger 100 by high pressure nitrogen transfer lime 10 with sky, an end of high pressure nitrogen transfer lime 11 is connected with the condensation of interchanger 100 outlet 121, and condensation entrance 120 is communicated with condensation outlet 121.
The other end of high pressure nitrogen transfer lime 11 is connected with the condensation entrance 220 of interchanger 200, and an end of high pressure nitrogen transfer lime 12 is connected with the condensation of interchanger 200 outlet 221, and condensation entrance 220 is communicated with condensation outlet 221.
The other end of high pressure nitrogen transfer lime 12 is connected with the condensation entrance 320 of interchanger 300; High pressure low temperature liquid nitrogen transfer lime 20,21 is told in the condensation outlet 321 of interchanger 300, and condensation entrance 320 is communicated with condensation outlet 321.
Behind series connection one reducing valve 22, the other end is connected to the re-heat entrance 330 of interchanger 300 on the high pressure low temperature liquid nitrogen transfer lime 21, and high pressure low temperature liquid nitrogen transfer lime 20 the other ends are connected to the high pressure low temperature liquid nitrogen entrance 410 on nitrogen wash column 400 tops.
The raw hydrogen transfer lime 30 that is connected with molecular sieve is connected with the condensation entrance 210 of interchanger 200, and an end of raw hydrogen transfer lime 31 is connected with the condensation of interchanger 200 outlet 211, and condensation entrance 210 is communicated with condensation outlet 211.
The other end of raw hydrogen transfer lime 31 is connected with the condensation entrance 310 of interchanger 300, one end of raw hydrogen transfer lime 32 is connected with the condensation of interchanger 300 outlet 311, condensation entrance 310 is communicated with condensation outlet 311, and the other end of raw hydrogen transfer lime 32 is connected with the raw hydrogen entrance 810 on unstripped gas flash tank 800 tops.
Unstripped gas flash tank 800 cats head are provided with gaseous phase outlet 820, be provided with liquid-phase outlet 830 at the bottom of the tower, gaseous phase outlet 820 is connected by the gas phase entrance 420 of gas-phase transport pipe 40 with nitrogen wash column 400 bottoms, liquid-phase outlet 830 is connected with the re-heat entrance 340 of interchanger 300 by liquid phase transfer lime 41, the re-heat outlet 341 of interchanger 300 is connected with the liquid phase entrance 510 on methane rectifying tower 500 tops by liquid phase transfer lime 43, and re-heat entrance 340 is communicated with re-heat outlet 341.Be serially connected with constant enthalpy reducing valve 42 on the liquid phase transfer lime 41.
Be provided with at the cat head of nitrogen wash column 400 and remove CO, Ar, CH 4 Gaseous phase outlet 430 behind the impurity, be provided with liquid rich CO cut outlet 440 at the bottom of the tower, gaseous phase outlet 430 is connected with the re-heat entrance 350 of interchanger 300 by gas-phase transport pipe 50, re-heat outlet 351 and the re-heat entrance 330 of interchanger 300,350 are communicated with, the re-heat of interchanger 300 outlet 351 is connected with the re-heat entrance 240 of interchanger 200 by gas-phase transport pipe 51, virgin gas transfer lime 60 is told in the re-heat outlet 241 of interchanger 200,61, the other end of virgin gas transfer lime 60 is connected with the entrance of methane rectifying tower 500 tower bottom reboilers 700, and the outlet of methane rectifying tower tower bottom reboiler 700 connects low-temperature rectisol workshop section 1200 by virgin gas transfer lime 62.The other end of virgin gas transfer lime 61 connects the re-heat entrance 140 of interchanger 100, and the re-heat outlet 141 of interchanger 100 connects ammonia synthesis workshop section 1300 by virgin gas transfer lime 63, and re-heat entrance 140 is communicated with re-heat outlet 141; Low-temperature rectisol workshop section 1200 also is connected with virgin gas transfer lime 63 by virgin gas return tube 64.
Liquid rich CO cut outlet 440 at the bottom of nitrogen wash column 400 towers is connected to the entrance 910 of C0 rich solution tank 900 by the rich CO cut of liquid state transfer lime 70, the top of C0 rich solution tank 900 is provided with gaseous phase outlet 920, and the bottom is provided with liquid-phase outlet 930; Be serially connected with constant enthalpy reducing valve 79 on the liquid rich CO cut transfer lime 70.
Liquid-phase outlet 930 is connected with the cold junction entrance of methane rectifying tower cat head condenser 600 by liquid phase transfer lime 72, the cold side outlet of methane rectifying tower cat head condenser 600 connects an end of gas-phase transport pipe 71, gaseous phase outlet 920 connects an end of gas-phase transport pipe 73, the other end of the other end of gas-phase transport pipe 73 and gas-phase transport pipe 71 and connect after be connected with the re-heat entrance 360 of interchanger 300 by gas-phase transport arm 75, one end of exhaust pipe 76 is connected with the re-heat of interchanger 300 outlet 361, and re-heat entrance 360 is communicated with re-heat outlet 361; The other end of exhaust pipe 76 is connected with the re-heat entrance 230 of interchanger 200, one end of exhaust pipe 77 is connected with the re-heat of interchanger 200 outlet 231, re-heat outlet 231 is communicated with re-heat entrance 230, the other end of exhaust pipe 77 is connected with the re-heat entrance 130 of interchanger 100, one end of exhaust pipe 78 is connected with the re-heat of interchanger 100 outlet 131, re-heat outlet 131 is communicated with another termination gas ductwork 1400 of exhaust pipe 78 with re-heat entrance 130.
The cat head of methane rectifying tower 500 is provided with gaseous phase outlet 520, be provided with methane rich liquid phase outlet 530 at the bottom of the tower, methane rectifying tower cat head condenser 600 is as for outside the methane rectifying tower 500, gaseous phase outlet 520 is connected by the hot junction entrance of gas-phase transport pipe 80 with methane rectifying tower cat head condenser 600, and the hot junction outlet of methane rectifying tower cat head condenser 600 is connected with the entrance 1510 of methane rectifying tower return tank 1500; Top at methane rectifying tower return tank 1500 is provided with gaseous phase outlet 1520, and the bottom is provided with bypass outlet 1530; Be provided with reflux inlet 540 on the top of methane rectifying tower 500, gaseous phase outlet 1520 is connected with exhaust pipe 76 by gas-phase transport pipe 90; Bypass outlet 1530 is connected with the reflux inlet 540 on methane rectifying tower 500 tops by return line 91.
The methane rich liquid phase outlet 530 of methane rectifying tower 500 bottoms connects the re-heat entrance 250 of interchanger 200 by methane rich liquid phase transfer lime 92, one end of methane rich liquid phase transfer lime 93 is connected to the re-heat outlet 251 of interchanger 200, re-heat outlet 251 is communicated with re-heat entrance 250, the other end of methane rich liquid phase transfer lime 93 is connected to the re-heat entrance 150 of interchanger 100, the re-heat of interchanger 100 outlet 151 is connected to SNG storage tank 1600 by SNG line of pipes 94, and re-heat outlet 151 is communicated with re-heat entrance 150.
The methane rich liquid phase outlet 530 of methane rectifying tower 500 bottoms also is connected with a methane rich liquid phase transfer lime 95, this methane rich liquid phase transfer lime 95 is connected with the entrance of liquid methane pump 1000, the outlet of liquid methane pump 1000 is connected to the re-heat entrance 260 of interchanger 200 by methane rich liquid phase transfer lime 96, the re-heat outlet 261 of interchanger 200 is connected to the re-heat entrance 160 of interchanger 100 by methane rich liquid phase transfer lime 97, re-heat outlet 261 is communicated with re-heat entrance 260, and the re-heat of interchanger 100 exports 161 and is connected to the workshop section 1700 of gasifying by high-pressure gas transfer lime 98; Re-heat outlet 161 is communicated with re-heat entrance 160.
Be provided with liquid nitrogen in the bottom of C0 rich solution tank 900 and replenish mouth 940, this liquid nitrogen replenishes mouth 940 and replenishes pipe 941 connecting fluid nitrogenous sources by liquid nitrogen.
The technical process of this embodiment is as follows: the raw hydrogen from molecular sieve enters interchanger 200 interior coolings by raw hydrogen transfer lime 30, and then enter interchanger 300 interior further coolings by raw hydrogen transfer lime 31, be-180～-190 ℃ by interchanger 300 raw hydrogen temperature out.The raw hydrogen of this temperature is sent into the 800 interior flash distillations of raw material flash tank by raw hydrogen transfer lime 32, and the gas phase after the flash distillation is flowed out by the tank deck of raw material flash tank 800, enters into nitrogen wash column 400 bottoms by gas-phase transport pipe 40.
The medium pressure nitrogen gas that divides from sky forms high pressure nitrogen after through the nitrogen compressor compression, high pressure nitrogen enters interchanger 100 interior coolings by high pressure nitrogen transfer lime 10, send into interchanger 200 interior further coolings through interchanger 100 cooled high pressure nitrogens by high pressure nitrogen transfer lime 11, send into again step cooling in the interchanger 300 through interchanger 200 further cooled high pressure nitrogens by high pressure nitrogen transfer lime 12, final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.
By interchanger 300 high pressure low temperature liquid nitrogen out by being divided into two strands, one high pressure low temperature liquid nitrogen is directly sent into nitrogen wash column 400 inside by high pressure low temperature liquid nitrogen transfer lime 20 by nitrogen wash column 400 tops, with enter after the nitrogen wash column 400 interior flash distillations the gas phase counter current contact, remove CO, Ar, CH in the gas phase after the flash distillation 4Impurity forms and removes CO, Ar, CH 4Gas phase behind the impurity and liquid rich CO cut.Remove CO, Ar, CH 4Gas phase behind the impurity meets the ammonia synthesis catalyst requirement.
Remove CO, Ar, CH 4Gas phase behind the impurity is flowed out by nitrogen wash column 400 cats head, sends into interchanger 300 re-heats by gas-phase transport pipe 50; Another strand returns interchanger 300 cold junction re-heats by high pressure low temperature liquid nitrogen transfer lime 21 and after reducing valve 22 decompression, and removes CO, Ar, CH after the re-heat 4Form virgin gas after gas phase behind the impurity is mixed, the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.
Virgin gas is sent into interchanger 200 interior further re-heats by virgin gas transfer lime 51 again, and to become temperature be-45～-65 ℃ virgin gas; This virgin gas is divided into two strands, one is delivered to by virgin gas transfer lime 60, and to obtain temperature after reboiler 700 coolings at the bottom of the methane rectifying tower be-50～-70 ℃ virgin gas, and then delivering to low-temperature rectisol workshop section 1200 re-heats to temperature by virgin gas transfer lime 62 is 25～35 ℃ of virgin gases; Another burst virgin gas is sent into interchanger 100 re-heats by virgin gas transfer lime 61, formation temperature is 25～35 ℃ of virgin gases, sends into synthetic ammonia workshop section 1300 by virgin gas transfer lime 63 after this virgin gas is mixed with the virgin gas that low-temperature rectisol workshop section 1200 brings by virgin gas return tube 64.
Liquid phase after the flash distillation is gone out by the tank underflow of raw material flash tank 800, after process constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, turn back to by liquid phase transfer lime 41 and to carry out re-heat in the interchanger 300, re-heat is entered in the methane rectifying tower 500 by methane rectifying tower 500 cats head by liquid phase transfer lime 43 after-150～-160 ℃, by making with extra care of methane rectifying tower 500, the methane rich liquid phase that meets related request is gone out by the tower bottom flow of methane rectifying tower 500, and the gas phase after the rectifying is flowed out by the cat head of methane rectifying tower 500.The methane rich liquid phase volumetric molar concentration that is gone out by the tower bottom flow of methane rectifying tower 500 is greater than 95%, and the rate of recovery of methane rectifying tower 500 is greater than 90%.
Consider that vapourizing furnace needs fuel under high pressure when normally moving, the methane rich liquid phase that is gone out by the tower bottom flow of methane rectifying tower 500 is divided into two strands, after one sends into interchanger 200 interior recovery cold re-heats by methane rich liquid phase transfer lime 92, send into interchanger 100 interior recovery cold re-heats by methane rich liquid phase transfer lime 93 again and to 25～35 ℃ of SNG delivery temperatures, deliver to SNG storage tank 1600.Another strand is by sending into interchanger 200 re-heats by methane rich liquid phase transfer lime 96 after 1000 superchargings of liquid methane pump, after interchanger 200 re-heats, send into interchanger 100 further re-heats by methane rich liquid phase transfer lime 97 again and form high-pressure gas, be connected to gasification workshop section 1700 by high-pressure gas transfer lime 98.
The liquid rich CO cut that is gone out by the tower bottom flow of nitrogen wash column 400 is after constant enthalpy reducing valve 79 constant enthalpys are decompressed to 0.25～0.35MPa, deliver in the carbon monoxide rich solution tank 900 by the rich CO cut of liquid state transfer lime 70 and to carry out flash distillation, formation temperature is-180～-195 ℃ liquid and gas after the flash distillation, liquid phase is gone out by carbon monoxide rich solution tank 900 tank underflows, deliver to condenser 600 cold junctions of methane rectifying tower 500 cats head by liquid phase transfer lime 72, for it returns after cold is provided, after the gas phase of bringing by gas-phase transport pipe 73 is mixed, send into by gas-phase transport arm 75 and to send by exhaust pipe 76 after colds are reclaimed in the interior re-heats of interchanger 300, with mix by the gas phase after the 1500 gas-liquid flash distillations of gas-phase transport pipe 90 methane rectifying tower return tanks after send into the interior further re-heats of interchanger 200 and reclaim colds, send in the interchanger 100 an again step re-heat by exhaust pipe 77 again and reclaim behind the cold as combustion gas, send into gas ductwork 1400 by exhaust pipe 78.
Send into condenser 600 hot junctions by the gas phase after the cat head outflow rectifying of methane rectifying tower 500 by gas-phase transport pipe 80, with enter after-180～-195 ℃ liquid phase in the condenser 600 carries out the heat exchange condensation, send into methane rectifying tower return tank 1500 and carry out the gas-liquid flash distillation, liquid phase after the gas-liquid flash distillation as methane rectifying tower 500 trim the top of column, adopts total reflux by return line 91.
Above-mentioned coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies preparation ammonia synthetic fresh gas coproduction SNG and high-pressure gas technique is only produced the product of SNG specification, whole device low temperature cold measures reasonable utilization, the self cooling balance of whole device need not out-of-bounds to input cold in the normal productive process.But, consider the fluctuation of production process, the drawback that may exist in the operation, the method is replenished pipe 941 to carbon monoxide rich solution tank 900 interior additional liquid nitrogen by liquid nitrogen, the cold deficiency that may cause to eliminate above-mentioned reason.
Embodiment 2
Referring to Fig. 5, Fig. 5 has provided coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies the another kind of device schema of preparing ammonia synthetic fresh gas and coproduction SNG.
The difference of this embodiment and embodiment 1 is exactly: the other end of high pressure nitrogen transfer lime 12 is told two strands, one high pressure nitrogen transfer lime 12a is connected with the condensation entrance 320 of interchanger 300, and another strand high pressure nitrogen transfer lime 12b directly is connected with virgin gas transfer lime 51.High pressure low temperature liquid nitrogen transfer lime 20 is told in 321 of the condensation outlets of interchanger 300, does not tell high pressure low temperature liquid nitrogen transfer lime 21.Interchanger 300 lacks re-heat entrance 330,340 and re-heat outlet 341, and liquid phase transfer lime 41 directly is connected to unite two into one with liquid phase transfer lime 43 and directly is connected with the liquid phase entrance 510 on methane rectifying tower 500 tops, and rest part is identical with embodiment 1.This embodiment can guarantee interchanger 200,300 load and the equilibrium of equipment size, to directly enter into methane rectifying tower 500 from the liquid phase of unstripped gas flash tank 800, after reclaiming high density methane, SNG and tail gas are delivered to respectively SNG storage tank and fuel gas pipe network by re-heat respectively, if the methane rectifying tower adopts this distributing style, for rationally utilizing energy, can adopt the high pressure nitrogen of the second heat exchanger exit as the thermal source of methane rectifying tower, and the cold of methane rectifying tower cat head condenser still come from the liquid phase of carbon monoxide rich solution tank.
The process distinction of this embodiment and embodiment is: be divided into two strands through interchanger 200 further cooled high pressure nitrogens, one sends into again step cooling in the interchanger 300 by high pressure nitrogen transfer lime 12a, and final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.Remove CO, Ar, CH 4Gas phase behind the impurity is flowed out by nitrogen wash column 400 cats head, sends into interchanger 300 re-heats by gas-phase transport pipe 50, removes CO, Ar, CH after the re-heat 4Form virgin gas after gas phase behind the impurity is mixed with another strand high pressure nitrogen that high pressure nitrogen transfer lime 12b brings, the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.Liquid phase after the flash distillation is gone out by the tank underflow of raw material flash tank 800, after process constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, do not need to turn back to by liquid phase transfer lime 41 and carry out re-heat in the interchanger 300, make with extra care but directly entered in the methane rectifying tower 500 by methane rectifying tower 500 cats head by liquid phase transfer lime 43.
Embodiment 3:
Referring to Fig. 6, Fig. 6 has provided coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies a kind of device schema of preparing ammonia synthetic fresh gas and coproduction LNG.
This coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies the device of preparation ammonia synthetic fresh gas coproduction LNG and high-pressure gas, comprises interchanger 100,200,300, nitrogen wash column 400, methane rectifying tower 500, methane rectifying tower cat head condenser 600, methane rectifying tower tower bottom reboiler 700, unstripped gas flash tank 800, C0 rich solution tank 900, liquid methane pump 1000, methane rectifying tower return tank 1500.
Divide the nitrogen compressor 1100 that is connected to be connected with the condensation entrance 120 of interchanger 100 by high pressure nitrogen transfer lime 10 with sky, an end of high pressure nitrogen transfer lime 11 is connected with the condensation of interchanger 100 outlet 121, and condensation entrance 120 is communicated with condensation outlet 121.
The other end of high pressure nitrogen transfer lime 11 is connected with the condensation entrance 220 of interchanger 200, and an end of high pressure nitrogen transfer lime 12 is connected with the condensation of interchanger 200 outlet 221, and condensation entrance 220 is communicated with condensation outlet 221.
The other end of high pressure nitrogen transfer lime 12 is connected with the condensation entrance 320 of interchanger 300; High pressure low temperature liquid nitrogen transfer lime 20,21 is told in the condensation outlet 321 of interchanger 300, and condensation entrance 320 is communicated with condensation outlet 321.
Behind series connection one reducing valve 22, the other end is connected to the re-heat entrance 330 of interchanger 300 on the high pressure low temperature liquid nitrogen transfer lime 21, and high pressure low temperature liquid nitrogen transfer lime 20 the other ends are connected to the high pressure low temperature liquid nitrogen entrance 410 on nitrogen wash column 400 tops.
The raw hydrogen transfer lime 30 that is connected with molecular sieve is connected with the condensation entrance 210 of interchanger 200, and an end of raw hydrogen transfer lime 31 is connected with the condensation of interchanger 200 outlet 211, and condensation entrance 210 is communicated with condensation outlet 211.
The other end of raw hydrogen transfer lime 31 is connected with the condensation entrance 310 of interchanger 300, one end of raw hydrogen transfer lime 32 is connected with the condensation of interchanger 300 outlet 311, condensation entrance 310 is communicated with condensation outlet 311, and the other end of raw hydrogen transfer lime 32 is connected with the raw hydrogen entrance 810 on unstripped gas flash tank 800 tops.
Unstripped gas flash tank 800 cats head are provided with gaseous phase outlet 820, be provided with liquid-phase outlet 830 at the bottom of the tower, gaseous phase outlet 820 is connected by the gas phase entrance 420 of gas-phase transport pipe 40 with nitrogen wash column 400 bottoms, liquid-phase outlet 830 is connected with the re-heat entrance 340 of interchanger 300 by liquid phase transfer lime 41, the re-heat outlet 341 of interchanger 300 is connected with the liquid phase entrance 510 on methane rectifying tower 500 tops by liquid phase transfer lime 43, and re-heat entrance 340 is communicated with re-heat outlet 341.Be serially connected with constant enthalpy reducing valve 42 on the liquid phase transfer lime 41.
Be provided with at the cat head of nitrogen wash column 400 and remove CO, Ar, CH 4 Gaseous phase outlet 430 behind the impurity, be provided with liquid rich CO cut outlet 440 at the bottom of the tower, gaseous phase outlet 430 is connected with the re-heat entrance 350 of interchanger 300 by gas-phase transport pipe 50, re-heat outlet 351 and the re-heat entrance 330 of interchanger 300,350 are communicated with, the re-heat of interchanger 300 outlet 351 is connected with the re-heat entrance 240 of interchanger 200 by gas-phase transport pipe 51, virgin gas transfer lime 60 is told in the re-heat outlet 241 of interchanger 200,61, the other end of virgin gas transfer lime 60 is connected with the entrance of methane rectifying tower 500 tower bottom reboilers 700, and the outlet of methane rectifying tower tower bottom reboiler 700 connects low-temperature rectisol workshop section 1200 by virgin gas transfer lime 62.The other end of virgin gas transfer lime 61 connects the re-heat entrance 140 of interchanger 100, and the re-heat outlet 141 of interchanger 100 connects ammonia synthesis workshop section 1300 by virgin gas transfer lime 63, and re-heat entrance 140 is communicated with re-heat outlet 141; Low-temperature rectisol workshop section 1200 also is connected with virgin gas transfer lime 63 by virgin gas return tube 64.
Liquid rich CO cut outlet 440 at the bottom of nitrogen wash column 400 towers is connected to the entrance 910 of C0 rich solution tank 900 by the rich CO cut of liquid state transfer lime 70, the top of C0 rich solution tank 900 is provided with gaseous phase outlet 920, and the bottom is provided with liquid-phase outlet 930; Be serially connected with constant enthalpy reducing valve 79 on the liquid rich CO cut transfer lime 70.
Liquid-phase outlet 930 is connected with the cold junction entrance of methane rectifying tower cat head condenser 600 by liquid phase transfer lime 72, the cold side outlet of methane rectifying tower cat head condenser 600 connects an end of gas-phase transport pipe 71, gaseous phase outlet 930 connects an end of gas-phase transport pipe 73, the other end of the other end of gas-phase transport pipe 73 and gas-phase transport pipe 71 and connect after be connected with the re-heat entrance 360 of interchanger 300 by gas-phase transport arm 75, one end of exhaust pipe 76 is connected with the re-heat of interchanger 300 outlet 361, and re-heat entrance 360 is communicated with re-heat outlet 361; The other end of exhaust pipe 76 is connected with the re-heat entrance 230 of interchanger 200, one end of exhaust pipe 77 is connected with the re-heat of interchanger 200 outlet 231, re-heat outlet 231 is communicated with re-heat entrance 230, the other end of exhaust pipe 77 is connected with the re-heat entrance 130 of interchanger 100, one end of exhaust pipe 78 is connected with the re-heat of interchanger 100 outlet 131, re-heat outlet 131 is communicated with another termination gas ductwork 1400 of exhaust pipe 78 with re-heat entrance 130.
The cat head of methane rectifying tower 500 is provided with gaseous phase outlet 520, be provided with methane rich liquid phase outlet 530 at the bottom of the tower, methane rectifying tower cat head condenser 600 is as for outside the methane rectifying tower 500, gaseous phase outlet 520 is connected by the hot junction entrance of gas-phase transport pipe 80 with methane rectifying tower cat head condenser 600, and the hot junction outlet of methane rectifying tower cat head condenser 600 is connected with the entrance 1510 of methane rectifying tower return tank 1500; Top at methane rectifying tower return tank 1500 is provided with gaseous phase outlet 1520, and the bottom is provided with bypass outlet 1530; Be provided with reflux inlet 540 on the top of methane rectifying tower 500, gaseous phase outlet 1520 is connected with exhaust pipe 76 by gas-phase transport pipe 90; Bypass outlet 1530 is connected with the reflux inlet 540 on methane rectifying tower 500 tops by return line 91.
The methane rich liquid phase outlet 530 of methane rectifying tower 500 bottoms is connected to the entrance of liquid methane pump 1000 by methane rich liquid phase transfer lime 92a, the outlet of liquid methane pump 1000 meets methane rich liquid phase transfer lime 96,96a, be provided with reducing valve 96c, 96d at methane rich liquid phase transfer lime 96,96a, the other end of methane rich liquid phase transfer lime 96a is connected with the condensation entrance 370 of interchanger 300, and the condensation outlet 371 of interchanger 300 connects LNG storage tank 1800 by LNG transfer lime 96b; Methane rich liquid phase transfer lime 96 is connected with the re-heat entrance 260 of interchanger 200, the re-heat outlet 261 of interchanger 200 is connected to 160 re-heat entrances of interchanger 100 by methane rich liquid phase transfer lime 97, re-heat outlet 161 is communicated with re-heat entrance 160, and the re-heat of interchanger 100 exports 161 and is connected to the workshop section 1700 of gasifying by high-pressure gas transfer lime 98.
In only producing the LNG process, the situation of cold deficiency may appear, connect a Claude cycle refrigeration system at interchanger 100,200 for this reason, circulatory mediator is N 2This Claude cycle refrigeration system is by a compressor 1910, a decompressor 1920 and a water cooler 1930 form, wherein the entrance of compressor 1910 is connected with the cold loop exit 171 of interchanger 100, the outlet of compressor 1910 is connected with the hot junction entrance of water cooler 1930, the hot junction outlet of water cooler 1930 is connected with the cold loop head 180 of interchanger 100, the cold loop exit 181 of interchanger 100 is connected with the cold loop head 270 of interchanger 200, cold loop exit 181 is communicated with cold loop head 180, the cold loop exit 271 of interchanger 200 is connected with the entrance of decompressor 1920, the outlet of decompressor 1920 is connected with the cold loop head 280 of interchanger 200, the cold loop exit 281 of interchanger 200 is connected with the cold loop head 170 of interchanger 100, cold loop exit 280 is communicated with cold loop head 281, cold loop head 270 is communicated with cold loop head 271, and cold loop head 170 is communicated with cold loop exit 171.
The technical process of this embodiment is as follows: the raw hydrogen from molecular sieve enters interchanger 200 interior coolings by raw hydrogen transfer lime 30, and then enter interchanger 300 interior further coolings by raw hydrogen transfer lime 31, be-180～-190 ℃ by interchanger 300 raw hydrogen temperature out.The raw hydrogen of this temperature is sent into the 800 interior flash distillations of raw material flash tank by raw hydrogen transfer lime 32, and the gas phase after the flash distillation is flowed out by the tank deck of raw material flash tank 800, enters into nitrogen wash column 400 bottoms by gas-phase transport pipe 40.
The medium pressure nitrogen gas that divides from sky forms high pressure nitrogen after through nitrogen compressor 1100 compressions, high pressure nitrogen enters interchanger 100 interior coolings by high pressure nitrogen transfer lime 10, send into interchanger 200 interior further coolings through interchanger 100 cooled high pressure nitrogens by high pressure nitrogen transfer lime 11, send into again step cooling in the interchanger 300 through interchanger 200 further cooled high pressure nitrogens by high pressure nitrogen transfer lime 12, final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.
By interchanger 300 high pressure low temperature liquid nitrogen out by being divided into two strands, one high pressure low temperature liquid nitrogen is directly sent into nitrogen wash column 400 inside by high pressure low temperature liquid nitrogen transfer lime 20 by nitrogen wash column 400 tops, with the gas phase counter current contact that enters after the nitrogen wash column 400 interior flash distillations, remove CO, Ar, CH in the gas phase after the flash distillation 4Impurity forms and removes CO, Ar, CH 4Gas phase behind the impurity and liquid rich CO cut.Remove CO, Ar, CH 4Gas phase behind the impurity meets the ammonia synthesis catalyst requirement.
Remove CO, Ar, CH 4Gas phase behind the impurity is flowed out by nitrogen wash column 400 cats head, sends into interchanger 300 re-heats by gas-phase transport pipe 50; Another strand returns interchanger 300 cold junction re-heats by high pressure low temperature liquid nitrogen transfer lime 21 and after reducing valve 22 decompression, and removes CO, Ar, CH after the re-heat 4Form virgin gas after gas phase behind the impurity is mixed, the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.
Virgin gas is sent into interchanger 200 interior further re-heats by virgin gas transfer lime 51 again, and to become temperature be-45～-65 ℃ virgin gas; This virgin gas is divided into two strands, one is delivered to by virgin gas transfer lime 60, and to obtain temperature after reboiler 700 coolings at the bottom of the methane rectifying tower be-50～-70 ℃ virgin gas, and then delivering to low-temperature rectisol workshop section 1200 re-heats to temperature by virgin gas transfer lime 62 is 25～35 ℃ of virgin gases; Another burst virgin gas is sent into interchanger 100 re-heats by virgin gas transfer lime 61, formation temperature is 25～35 ℃ of virgin gases, sends into synthetic ammonia workshop section 1300 by virgin gas transfer lime 63 after this virgin gas is mixed with the virgin gas that low-temperature rectisol workshop section 1200 brings by virgin gas return tube 64.
Liquid phase after the flash distillation is gone out by the tank underflow of raw material flash tank 800, after process constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, turn back to by liquid phase transfer lime 41 and to carry out re-heat in the interchanger 300, re-heat is entered in the methane rectifying tower 500 by methane rectifying tower 500 cats head by liquid phase transfer lime 43 after-150～-160 ℃, by making with extra care of methane rectifying tower 500, the methane rich liquid phase that meets related request is gone out by the tower bottom flow of methane rectifying tower 500, and the gas phase after the rectifying is flowed out by the cat head of methane rectifying tower 500.The methane rich liquid phase volumetric molar concentration that is gone out by the tower bottom flow of methane rectifying tower 500 is greater than 95%, and the rate of recovery of methane rectifying tower 500 is greater than 90%.
Consider that vapourizing furnace needs fuel under high pressure when normally moving, be divided into two strands after methane rich liquid phase feed liquor methane pump 1000 pressurizations that gone out by the tower bottom flow of methane rectifying tower 500, one is by methane rich liquid phase transfer lime 96 and by sending into interchanger 200 re-heats after the reducing valve 96c decompression, after interchanger 200 re-heats, send into interchanger 100 further re-heats by methane rich liquid phase transfer lime 97 again and form high-pressure gas, be connected to gasification workshop section 1700 by high-pressure gas transfer lime 98.Another is strand by methane rich liquid phase transfer lime 96a and by sending into interchanger 300 condensations behind the variable valve 96d, delivers to LNG storage tank 1800 by LNG transfer lime 96b condense to the temperature that meets LNG accumulating requirement through interchanger 300 after.
The liquid rich CO cut that is gone out by the tower bottom flow of nitrogen wash column 400 is after constant enthalpy reducing valve 79 constant enthalpys are decompressed to 0.25～0.35MPa, deliver in the carbon monoxide rich solution tank 900 by the rich CO cut of liquid state transfer lime 70 and to carry out flash distillation, formation temperature is-180～-195 ℃ liquid and gas after the flash distillation, liquid phase is gone out by carbon monoxide rich solution tank 900 tank underflows, deliver to condenser 600 cold junctions of methane rectifying tower 500 cats head by liquid phase transfer lime 72, for it returns after cold is provided, after the gas phase of bringing by gas-phase transport pipe 73 is mixed, send into by gas-phase transport arm 75 and to send by exhaust pipe 76 after colds are reclaimed in the interior re-heats of interchanger 300, with mix by the gas phase after the 1500 gas-liquid flash distillations of gas-phase transport pipe 90 methane rectifying tower return tanks after send into the interior further re-heats of interchanger 200 and reclaim colds, send in the interchanger 100 an again step re-heat by exhaust pipe 77 again and reclaim behind the cold as combustion gas, send into gas ductwork 1400 by exhaust pipe 78.
Send into condenser 600 hot junctions by the gas phase after the cat head outflow rectifying of methane rectifying tower 500 by gas-phase transport pipe 80, with enter after-180～-195 ℃ liquid phase in the condenser 600 carries out the heat exchange condensation, send into methane rectifying tower return tank 1500 and carry out the gas-liquid flash distillation, liquid phase after the gas-liquid flash distillation as methane rectifying tower 500 trim the top of column, adopts total reflux by return line 91.
Above-mentioned coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies preparation ammonia synthetic fresh gas coproduction SNG and high-pressure gas technique is only produced the product of LNG specification, the low temperature cold of system can not satisfy the requirement of self, the Claude circularly cooling is produced the LNG product for system provides cold so need to come into operation, whole circulation loop adopts circulating water to take away heat, and need not out-of-bounds to input the low temperature cold, for example from the low temperature liquid nitrogen of air cooling device.
Embodiment 4
Referring to Fig. 7, Fig. 7 has provided coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies the another kind of device schema of preparing ammonia synthetic fresh gas and coproduction LNG.
The difference of this embodiment and embodiment 3 is exactly: the other end of high pressure nitrogen transfer lime 12 is told two strands, one high pressure nitrogen transfer lime 12a is connected with the condensation entrance 320 of interchanger 300, and another strand high pressure nitrogen transfer lime 12b directly is connected with virgin gas transfer lime 51.High pressure low temperature liquid nitrogen transfer lime 20 is told in 321 of the condensation outlets of interchanger 300, does not tell high pressure low temperature liquid nitrogen transfer lime 21.Interchanger 300 lacks re-heat entrance 330,340 and re-heat outlet 341, and liquid phase transfer lime 41 directly is connected to unite two into one with liquid phase transfer lime 43 and directly is connected with the liquid phase entrance 510 on methane rectifying tower 500 tops, and rest part is identical with embodiment 1.This embodiment can guarantee interchanger 200,300 load and the equilibrium of equipment size, to directly enter into methane rectifying tower 500 from the liquid phase of unstripped gas flash tank 800, after reclaiming high density methane, LNG then further is cooled to-162 ℃ through the 3rd interchanger and delivers to the LNG storage tank, and wherein the fuel under high pressure gas pipe network is delivered in the re-heat after the supercharging of liquid methane pump of the fuel under high pressure of by-product.If the methane rectifying tower adopts this distributing style, for rationally utilizing energy, can adopt the high pressure nitrogen of the second heat exchanger exit as the thermal source of methane rectifying tower, and the cold of methane rectifying tower cat head condenser still come from the liquid phase of carbon monoxide rich solution tank.
The process distinction of this embodiment and embodiment is: be divided into two strands through interchanger 200 further cooled high pressure nitrogens, one sends into again step cooling in the interchanger 300 by high pressure nitrogen transfer lime 12a, and final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.Remove CO, Ar, CH 4Gas phase behind the impurity is flowed out by nitrogen wash column 400 cats head, sends into interchanger 300 re-heats by gas-phase transport pipe 50, removes CO, Ar, CH after the re-heat 4Form virgin gas after gas phase behind the impurity is mixed with another strand high pressure nitrogen that high pressure nitrogen transfer lime 12b brings, the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.Liquid phase after the flash distillation is gone out by the tank underflow of raw material flash tank 800, after process constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, do not need to turn back to by liquid phase transfer lime 41 and carry out re-heat in the interchanger 300, make with extra care but directly entered in the methane rectifying tower 500 by methane rectifying tower 500 cats head by liquid phase transfer lime 43.
Embodiment 5:
Referring to Fig. 8, Fig. 8 has provided coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies a kind of device schema of preparing ammonia synthetic fresh gas and coproduction SNG and LNG.
This coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies the device of preparation ammonia synthetic fresh gas coproduction SNG LNG and high-pressure gas, comprises interchanger 100,200,300, nitrogen wash column 400, methane rectifying tower 500, methane rectifying tower cat head condenser 600, methane rectifying tower tower bottom reboiler 700, unstripped gas flash tank 800, C0 rich solution tank 900, liquid methane pump 1000, methane rectifying tower return tank 1500.
Divide the nitrogen compressor 1100 that is connected to be connected with the condensation entrance 120 of interchanger 100 by high pressure nitrogen transfer lime 10 with sky, an end of high pressure nitrogen transfer lime 11 is connected with the condensation of interchanger 100 outlet 121, and condensation entrance 120 is communicated with condensation outlet 121.
The other end of high pressure nitrogen transfer lime 11 is connected with the condensation entrance 220 of interchanger 200, and an end of high pressure nitrogen transfer lime 12 is connected with the condensation of interchanger 200 outlet 221, and condensation entrance 220 is communicated with condensation outlet 221.
The other end of high pressure nitrogen transfer lime 12 is connected with the condensation entrance 320 of interchanger 300; High pressure low temperature liquid nitrogen transfer lime 20,21 is told in the condensation outlet 321 of interchanger 300, and condensation entrance 320 is communicated with condensation outlet 321.
Behind series connection one reducing valve 22, the other end is connected to the re-heat entrance 330 of interchanger 300 on the high pressure low temperature liquid nitrogen transfer lime 21, and high pressure low temperature liquid nitrogen transfer lime 20 the other ends are connected to the high pressure low temperature liquid nitrogen entrance 410 on nitrogen wash column 400 tops.
The raw hydrogen transfer lime 30 that is connected with molecular sieve is connected with the condensation entrance 210 of interchanger 200, and an end of raw hydrogen transfer lime 31 is connected with the condensation of interchanger 200 outlet 211, and condensation entrance 210 is communicated with condensation outlet 211.
The other end of raw hydrogen transfer lime 31 is connected with the condensation entrance 310 of interchanger 300, one end of raw hydrogen transfer lime 32 is connected with the condensation of interchanger 300 outlet 311, condensation entrance 310 is communicated with condensation outlet 311, and the other end of raw hydrogen transfer lime 32 is connected with the raw hydrogen entrance 810 on unstripped gas flash tank 800 tops.
Unstripped gas flash tank 800 cats head are provided with gaseous phase outlet 820, be provided with liquid-phase outlet 830 at the bottom of the tower, gaseous phase outlet 820 is connected by the gas phase entrance 420 of gas-phase transport pipe 40 with nitrogen wash column 400 bottoms, liquid-phase outlet 830 is connected with the re-heat entrance 340 of interchanger 300 by liquid phase transfer lime 41, the re-heat outlet 341 of interchanger 300 is connected with the liquid phase entrance 510 on methane rectifying tower 500 tops by liquid phase transfer lime 43, and re-heat entrance 340 is communicated with re-heat outlet 341.Be serially connected with constant enthalpy reducing valve 42 on the liquid phase transfer lime 41.
Be provided with at the cat head of nitrogen wash column 400 and remove CO, Ar, CH 4 Gaseous phase outlet 430 behind the impurity, be provided with liquid rich CO cut outlet 440 at the bottom of the tower, gaseous phase outlet 430 is connected with the re-heat entrance 350 of interchanger 300 by gas-phase transport pipe 50, re-heat outlet 351 and the re-heat entrance 330 of interchanger 300,350 are communicated with, the re-heat of interchanger 300 outlet 351 is connected with the re-heat entrance 240 of interchanger 200 by gas-phase transport pipe 51, virgin gas transfer lime 60 is told in the re-heat outlet 241 of interchanger 200,61, the other end of virgin gas transfer lime 60 is connected with the entrance of methane rectifying tower 500 tower bottom reboilers 700, and the outlet of methane rectifying tower tower bottom reboiler 700 connects low-temperature rectisol workshop section 1200 by virgin gas transfer lime 62.The other end of virgin gas transfer lime 61 connects the re-heat entrance 140 of interchanger 100, and the re-heat outlet 141 of interchanger 100 connects ammonia synthesis workshop section 1300 by virgin gas transfer lime 63, and re-heat entrance 140 is communicated with re-heat outlet 141; Low-temperature rectisol workshop section 1200 also is connected with virgin gas transfer lime 63 by virgin gas return tube 64.
Liquid rich CO cut outlet 440 at the bottom of nitrogen wash column 400 towers is connected to the entrance 910 of C0 rich solution tank 900 by the rich CO cut of liquid state transfer lime 70, the top of C0 rich solution tank 900 is provided with gaseous phase outlet 920, and the bottom is provided with liquid-phase outlet 930; Be serially connected with constant enthalpy reducing valve 79 on the liquid rich CO cut transfer lime 70.
Liquid-phase outlet 930 is connected with the cold junction entrance of methane rectifying tower cat head condenser 600 by liquid phase transfer lime 72, the cold side outlet of methane rectifying tower cat head condenser 600 connects an end of gas-phase transport pipe 71, gaseous phase outlet 930 connects an end of gas-phase transport pipe 73, the other end of the other end of gas-phase transport pipe 73 and gas-phase transport pipe 71 and connect after be connected with the re-heat entrance 360 of interchanger 300 by gas-phase transport arm 75, one end of exhaust pipe 76 is connected with the re-heat of interchanger 300 outlet 361, and re-heat entrance 360 is communicated with re-heat outlet 361; The other end of exhaust pipe 76 is connected with the re-heat entrance 230 of interchanger 200, one end of exhaust pipe 77 is connected with the re-heat of interchanger 200 outlet 231, re-heat outlet 231 is communicated with re-heat entrance 230, the other end of exhaust pipe 77 is connected with the re-heat entrance 130 of interchanger 100, one end of exhaust pipe 78 is connected with the re-heat of interchanger 100 outlet 131, re-heat outlet 131 is communicated with another termination gas ductwork 1400 of exhaust pipe 78 with re-heat entrance 130.
The cat head of methane rectifying tower 500 is provided with gaseous phase outlet 520, be provided with methane rich liquid phase outlet 530 at the bottom of the tower, methane rectifying tower cat head condenser 600 is as for outside the methane rectifying tower 500, gaseous phase outlet 520 is connected by the hot junction entrance of gas-phase transport pipe 80 with methane rectifying tower cat head condenser 600, and the hot junction outlet of methane rectifying tower cat head condenser 600 is connected with the entrance 1510 of methane rectifying tower return tank 1500; Top at methane rectifying tower return tank 1500 is provided with gaseous phase outlet 1520, and the bottom is provided with bypass outlet 1530; Be provided with reflux inlet 540 on the top of methane rectifying tower 500, gaseous phase outlet 1520 is connected with exhaust pipe 76 by gas-phase transport pipe 90; Bypass outlet 1530 is connected with the reflux inlet 540 on methane rectifying tower 500 tops by return line 91.
Consider that vapourizing furnace needs fuel under high pressure when normally moving, the methane rich liquid phase outlet 530 of methane rectifying tower 500 bottoms also is connected to methane rich liquid phase transfer lime 92,92a, be provided with variable valve 92b at methane rich liquid phase transfer lime 92, the other end of methane rich liquid phase transfer lime 92b is connected with the re-heat entrance 250 of interchanger 200, one end of methane rich liquid phase transfer lime 93 is connected to the re-heat outlet 251 of interchanger 200, re-heat outlet 251 is communicated with re-heat entrance 250, the other end of methane rich liquid phase transfer lime 93 is connected to the re-heat entrance 150 of interchanger 100, the re-heat of interchanger 100 outlet 151 is connected to SNG storage tank 1600 by SNG line of pipes 94, and re-heat outlet 151 is communicated with re-heat entrance 150.
Methane rich liquid phase transfer lime 92a is connected to the entrance of liquid methane pump 1000, the outlet of liquid methane pump 1000 meets methane rich liquid phase transfer lime 96,96a, be provided with variable valve 96c, 96d at methane rich liquid phase transfer lime 96,96a, SNG and LNG product structure are regulated and can be regulated by the flow that is distributed on methane rich liquid phase transfer lime 92, the 92a.
The other end of methane rich liquid phase transfer lime 96a is connected with the condensation entrance 370 of interchanger 300, and the condensation outlet 371 of interchanger 300 connects LNG storage tank 1800 by LNG transfer lime 96b; Methane rich liquid phase transfer lime 96 is connected with the re-heat entrance 260 of interchanger 200, the re-heat outlet 261 of interchanger 200 is connected to 160 re-heat entrances of interchanger 100 by methane rich liquid phase transfer lime 97, re-heat outlet 161 is communicated with re-heat entrance 160, and the re-heat of interchanger 100 exports 161 and is connected to the workshop section 1700 of gasifying by high-pressure gas transfer lime 98.Adopt this structure, can omit a methane rich compressor.
Because the device of the present embodiment can be produced the product of SNG and two kinds of specifications of LNG simultaneously, the low temperature cold of system can not satisfy the requirement of self, the Claude circularly cooling is that system replenishes cold for system provides cold or replenishes pipe 941 adding liquid nitrogen in carbon monoxide rich solution tank 940 by liquid nitrogen so need to come into operation, perhaps utilize simultaneously the Claude circularly cooling and produce LNG product in the mode of carbon monoxide rich solution tank 940 fluid infusion nitrogen for system replenishes cold by the additional pipe 941 of liquid nitrogen, for this reason at interchanger 100,200 connect a Claude cycle refrigeration system, and circulatory mediator is N 2This Claude cycle refrigeration system is by a compressor 1910, a decompressor 1920 and a water cooler 1930 form, wherein the entrance of compressor 1910 is connected with the cold loop exit 171 of interchanger 100, the outlet of compressor 1910 is connected with the hot junction entrance of water cooler 1930, the hot junction outlet of water cooler 1930 is connected with the cold loop head 180 of interchanger 100, the cold loop exit 181 of interchanger 100 is connected with the cold loop head 270 of interchanger 200, cold loop exit 181 is communicated with cold loop head 180, the cold loop exit 271 of interchanger 200 is connected with the entrance of decompressor 1920, the outlet of decompressor 1920 is connected with the cold loop head 280 of interchanger 200, the cold loop exit 281 of interchanger 200 is connected with the cold loop head 170 of interchanger 100, cold loop exit 280 is communicated with cold loop head 281, cold loop head 270 is communicated with cold loop head 271, and cold loop head 170 is communicated with cold loop exit 171.
The technical process of this embodiment is as follows: the raw hydrogen from molecular sieve enters interchanger 200 interior coolings by raw hydrogen transfer lime 30, and then enter interchanger 300 interior further coolings by raw hydrogen transfer lime 31, be-180～-190 ℃ by interchanger 300 raw hydrogen temperature out.The raw hydrogen of this temperature is sent into the 800 interior flash distillations of raw material flash tank by raw hydrogen transfer lime 32, and the gas phase after the flash distillation is flowed out by the tank deck of raw material flash tank 800, enters into nitrogen wash column 400 bottoms by gas-phase transport pipe 40.
The medium pressure nitrogen gas that divides from sky forms high pressure nitrogen after through nitrogen compressor 1100 compressions, high pressure nitrogen enters interchanger 100 interior coolings by high pressure nitrogen transfer lime 10, send into interchanger 200 interior further coolings through interchanger 100 cooled high pressure nitrogens by high pressure nitrogen transfer lime 11, send into again step cooling in the interchanger 300 through interchanger 200 further cooled high pressure nitrogens by high pressure nitrogen transfer lime 12, final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.
By interchanger 300 high pressure low temperature liquid nitrogen out by being divided into two strands, one high pressure low temperature liquid nitrogen is directly sent into nitrogen wash column 400 inside by high pressure low temperature liquid nitrogen transfer lime 20 by nitrogen wash column 400 tops, with the gas phase counter current contact that enters after the nitrogen wash column 400 interior flash distillations, remove CO, Ar, CH in the gas phase after the flash distillation 4Impurity forms and removes CO, Ar, CH 4Gas phase behind the impurity and liquid rich CO cut.Remove CO, Ar, CH 4Gas phase behind the impurity meets the ammonia synthesis catalyst requirement.
Remove CO, Ar, CH 4Gas phase behind the impurity is flowed out by nitrogen wash column 400 cats head, sends into interchanger 300 re-heats by gas-phase transport pipe 50; Another strand returns interchanger 300 cold junction re-heats by high pressure low temperature liquid nitrogen transfer lime 21 and after reducing valve 22 decompression, and removes CO, Ar, CH after the re-heat 4Form virgin gas after gas phase behind the impurity is mixed, the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.
Virgin gas is sent into interchanger 200 interior further re-heats by virgin gas transfer lime 51 again, and to become temperature be-45～-65 ℃ virgin gas; This virgin gas is divided into two strands, one is delivered to by virgin gas transfer lime 60, and to obtain temperature after reboiler 700 coolings at the bottom of the methane rectifying tower be-50～-70 ℃ virgin gas, and then delivering to low-temperature rectisol workshop section 1200 re-heats to temperature by virgin gas transfer lime 62 is 25～35 ℃ of virgin gases; Another burst virgin gas is sent into interchanger 100 re-heats by virgin gas transfer lime 61, formation temperature is 25～35 ℃ of virgin gases, sends into synthetic ammonia workshop section 1300 by virgin gas transfer lime 63 after this virgin gas is mixed with the virgin gas that low-temperature rectisol workshop section 1200 brings by virgin gas return tube 64.
Liquid phase after the flash distillation is gone out by the tank underflow of raw material flash tank 830, after process constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, turn back to by liquid phase transfer lime 41 and to carry out re-heat in the interchanger 300, re-heat is entered in the methane rectifying tower 500 by methane rectifying tower 500 cats head by liquid phase transfer lime 43 after-150～-160 ℃, by making with extra care of methane rectifying tower 500, the methane rich liquid phase that meets related request is gone out by the tower bottom flow of methane rectifying tower 500, and the gas phase after the rectifying is flowed out by the cat head of methane rectifying tower 500.The methane rich liquid phase volumetric molar concentration that is gone out by the tower bottom flow of methane rectifying tower 500 is greater than 95%, and the rate of recovery of methane rectifying tower 500 is greater than 90%.
Consider that vapourizing furnace needs fuel under high pressure when normally moving, the methane rich liquid phase that is gone out by the tower bottom flow of methane rectifying tower 500 is divided into two strands, after one sends into interchanger 200 interior recovery cold re-heats by methane rich liquid phase transfer lime 92, send into interchanger 200 interior recovery cold re-heats by methane rich liquid phase transfer lime 93 again and to 35 ℃ of SNG delivery temperatures, deliver to SNG storage tank 1600 by SNG transfer lime 94.Another strand is by being divided into two strands after 1000 superchargings of liquid methane pump, one is by methane rich liquid phase transfer lime 96 and by sending into interchanger 200 re-heats after the reducing valve 96c decompression, after interchanger 200 re-heats, send into interchanger 100 further re-heats by methane rich liquid phase transfer lime 97 again and form high-pressure gas, be connected to gasification workshop section 1700 by high-pressure gas transfer lime 98.Another strand sent into interchanger 300 condensations by methane rich liquid phase transfer lime 96a and by after the reducing valve 96d decompression, delivers to LNG storage tank 1800 by LNG transfer lime 96b condense to the temperature that meets LNG accumulating requirement through interchanger 300 after.
The liquid rich CO cut that is gone out by the tower bottom flow of nitrogen wash column 400 is after constant enthalpy reducing valve 79 constant enthalpys are decompressed to 0.25～0.35MPa, deliver in the carbon monoxide rich solution tank 900 by the rich CO cut of liquid state transfer lime 70 and to carry out flash distillation, formation temperature is-180～-195 ℃ liquid and gas after the flash distillation, liquid phase is gone out by carbon monoxide rich solution tank 900 tank underflows, deliver to condenser 600 cold junctions of methane rectifying tower 500 cats head by liquid phase transfer lime 72, for it returns after cold is provided, after the gas phase of bringing by gas-phase transport pipe 73 is mixed, send into by gas-phase transport arm 75 and to send by exhaust pipe 76 after colds are reclaimed in the interior re-heats of interchanger 300, with mix by the gas phase after the 1500 gas-liquid flash distillations of gas-phase transport pipe 90 methane rectifying tower return tanks after send into the interior further re-heats of interchanger 200 and reclaim colds, send in the interchanger 100 an again step re-heat by exhaust pipe 77 again and reclaim behind the cold as combustion gas, send into gas ductwork 1400 by exhaust pipe 78.
Send into condenser 600 hot junctions by the gas phase after the cat head outflow rectifying of methane rectifying tower 500 by gas-phase transport pipe 80, with enter after-180～-195 ℃ liquid phase in the condenser 600 carries out the heat exchange condensation, send into methane rectifying tower return tank 1500 and carry out the gas-liquid flash distillation, liquid phase after the gas-liquid flash distillation as methane rectifying tower 500 trim the top of column, adopts total reflux by return line 91.
Above-mentioned coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies preparation ammonia synthetic fresh gas coproduction SNG, LNG and high-pressure gas technique, the low temperature cold of system can not satisfy the requirement of self, the Claude circularly cooling is produced the LNG product for system provides cold so need to come into operation, whole circulation loop adopts circulating water to take away heat, and need not out-of-bounds to input the low temperature cold.But, consider the fluctuation of production process, the drawback that may exist in the operation, the method is replenished pipe 941 to carbon monoxide rich solution tank 900 interior additional liquid nitrogen by liquid nitrogen, the cold deficiency that may cause to eliminate above-mentioned reason.
Embodiment 6
Referring to Fig. 9, Fig. 9 has provided coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purifies the another kind of device schema of preparing ammonia synthetic fresh gas and coproduction SNG and LNG.
The difference of this embodiment and embodiment 3 is exactly: the other end of high pressure nitrogen transfer lime 12 is told two strands, one high pressure nitrogen transfer lime 12a is connected with the condensation entrance 320 of interchanger 300, and another strand high pressure nitrogen transfer lime 12b directly is connected with virgin gas transfer lime 51.High pressure low temperature liquid nitrogen transfer lime 20 is told in 321 of the condensation outlets of interchanger 300, does not tell high pressure low temperature liquid nitrogen transfer lime 21.Interchanger 300 lacks re-heat entrance 330,340 and re-heat outlet 341, and liquid phase transfer lime 41 directly is connected to unite two into one with liquid phase transfer lime 43 and directly is connected with the liquid phase entrance 510 on methane rectifying tower 500 tops, and rest part is identical with embodiment 1.
This embodiment can guarantee interchanger 200,300 load and the equilibrium of equipment size, to directly enter into methane rectifying tower 500 from the liquid phase of unstripped gas flash tank 800, after reclaiming high density methane, SNG and tail gas are delivered to respectively SNG storage tank and fuel gas pipe network by re-heat respectively, if production LNG then further is cooled to-162 ℃ through the 3rd interchanger and delivers to the LNG storage tank, wherein the fuel under high pressure gas pipe network is delivered in the re-heat after the supercharging of liquid methane pump of the fuel under high pressure of by-product.If the methane rectifying tower adopts this distributing style, for rationally utilizing energy, can adopt the high pressure nitrogen of the second heat exchanger exit as the thermal source of methane rectifying tower, and the cold of methane rectifying tower cat head condenser still come from the liquid phase of carbon monoxide rich solution tank.
The process distinction of this embodiment and embodiment is: be divided into two strands through interchanger 200 further cooled high pressure nitrogens, one sends into again step cooling in the interchanger 300 by high pressure nitrogen transfer lime 12a, and final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.Remove CO, Ar, CH 4Gas phase behind the impurity is flowed out by nitrogen wash column 400 cats head, sends into interchanger 300 re-heats by gas-phase transport pipe 50, removes CO, Ar, CH after the re-heat 4Form virgin gas after gas phase behind the impurity is mixed with another strand high pressure nitrogen that high pressure nitrogen transfer lime 12b brings, the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.Liquid phase after the flash distillation is gone out by the tank underflow of raw material flash tank 800, after process constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, do not need to turn back to by liquid phase transfer lime 41 and carry out re-heat in the interchanger 300, make with extra care but directly entered in the methane rectifying tower 500 by methane rectifying tower 500 cats head by liquid phase transfer lime 43.
Referring to Figure 10, in above-described embodiment, methane rectifying tower cat head condenser 600 can be built in the methane rectifying tower 500, the hot junction outlet of the gaseous phase outlet at methane rectifying tower 500 tops and methane rectifying tower cat head condenser 600 shares.

Claims (16)

1. coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, comprise First Heat Exchanger, the second interchanger, the 3rd interchanger and nitrogen wash column, it is characterized in that, also comprise methane rectifying tower, methane rectifying tower cat head condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, carbon monoxide rich solution tank, liquid methane pump;
Divide the first high pressure nitrogen transfer lime that is connected to be connected with the first condensation entrance of described First Heat Exchanger with sky, one end of the second high pressure nitrogen transfer lime is connected with the first condensation of described First Heat Exchanger outlet, the first condensation entrance is communicated with the first condensation outlet, the other end of the second high pressure nitrogen transfer lime is connected with the second condensation entrance of described the second interchanger, third high presses an end of nitrogen transfer lime to be connected with the second condensation outlet of described the second interchanger, the second condensation entrance is communicated with the second condensation outlet, third high presses the other end of nitrogen transfer lime to be divided into two strands, and one third high presses the nitrogen transfer lime to be connected with the 3rd condensation entrance of described the 3rd interchanger; The 3rd condensation outlet of described the 3rd interchanger connects an end of the first high pressure low temperature liquid nitrogen transfer lime, and the 3rd condensation entrance is communicated with the 3rd condensation outlet, and the first high pressure low temperature liquid nitrogen transfer lime is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top;
The the first raw hydrogen transfer lime that is connected with molecular sieve is connected with the 4th condensation entrance of described the second interchanger, one end of the second raw hydrogen transfer lime is connected with the 4th condensation of described the second interchanger outlet, the 4th condensation entrance is communicated with the 4th condensation outlet, the other end of the second raw hydrogen transfer lime is connected with the 5th condensation entrance of described the 3rd interchanger, one end of the 3rd raw hydrogen transfer lime is connected with the 5th condensation of described the 3rd interchanger outlet, the 5th condensation entrance is communicated with the 5th condensation outlet, and the other end of the 3rd raw hydrogen transfer lime is connected with the raw hydrogen entrance on described unstripped gas flash tank top;
Described unstripped gas flash tank cat head is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of the unstripped gas flash tank tower, the first gaseous phase outlet is connected with the first gas phase entrance of nitrogen wash column bottom by the first gas-phase transport pipe, and the first liquid-phase outlet is connected with the second liquid phase entrance of methane rectifier by the first liquid phase transfer lime;
Be provided with at the top of nitrogen wash column and remove CO, Ar, CH 4The second gaseous phase outlet behind the impurity, the bottom of nitrogen wash column is provided with liquid rich CO cut outlet, the second gaseous phase outlet connects by the 3rd re-heat entrance of the second gas-phase transport Guan Yudi three interchanger, the 3rd re-heat outlet of the 3rd interchanger is communicated with the 3rd re-heat entrance, the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe, and the second gas-phase transport pipe presses the nitrogen transfer lime to be connected with another burst third high; The 4th re-heat outlet of the second interchanger is the first virgin gas transfer lime, the first virgin gas transfer lime is divided into two strands, wherein the other end of one the first virgin gas transfer lime is connected with the entrance of described methane rectifying tower tower bottom reboiler, the outlet of methane rectifying tower tower bottom reboiler connects low-temperature rectisol workshop section entrance by the second virgin gas transfer lime, and the re-heat outlet of low-temperature rectisol workshop section connects the 3rd virgin gas transfer lime; The other end of another strand the first virgin gas transfer lime connects the 6th re-heat entrance of First Heat Exchanger, and the 6th re-heat outlet of First Heat Exchanger connects ammonia synthesis workshop section by the bright letter shoot of the "four news" (new ideas, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Described the 3rd virgin gas transfer lime is connected with the bright letter shoot of the described "four news" (new ideas;
The liquid rich CO cut outlet of nitrogen wash column bottom is connected to the entrance of carbon monoxide rich solution tank by the rich CO cut of liquid state transfer lime, the top of carbon monoxide rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of carbon monoxide rich solution tank is provided with the 3rd liquid-phase outlet; The 3rd liquid-phase outlet is connected with the cold junction entrance of methane rectifying tower cat head condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower cat head condenser connects an end of the 5th gas-phase transport pipe, the 4th gaseous phase outlet connects an end of the 4th gas-phase transport pipe, the other end of the other end of the 4th gas-phase transport pipe and the 5th gas-phase transport pipe and connect after the 7th re-heat entrance by the 6th gas-phase transport Guan Yudi three interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat of the 3rd interchanger outlet, and the 7th re-heat entrance is communicated with the 7th re-heat outlet; The other end of the first exhaust pipe is connected with the 8th re-heat entrance of the second interchanger, one end of the second exhaust pipe is connected with the 8th re-heat of the second interchanger outlet, the 8th re-heat outlet is communicated with the 8th re-heat entrance, the other end of the second exhaust pipe is connected with the 9th re-heat entrance of First Heat Exchanger, one end of the 3rd exhaust pipe is connected with the 9th re-heat of First Heat Exchanger outlet, the 9th re-heat outlet is communicated with another termination gas ductwork of the 3rd exhaust pipe with the 9th re-heat entrance;
The top of described methane rectifying tower is provided with the 3rd gaseous phase outlet, the bottom of methane rectifying tower is provided with the outlet of methane rich liquid phase, the 3rd gaseous phase outlet is connected with the hot junction entrance of described methane rectifying tower cat head condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower cat head condenser is connected with the 4th liquid phase transfer lime;
The methane rich liquid phase outlet of methane rectifier bottoms connects the tenth re-heat entrance of the second interchanger by the first methane rich liquid phase transfer lime, one end of the second methane rich liquid phase transfer lime is connected to the tenth re-heat outlet of the second interchanger, the tenth re-heat outlet is communicated with the tenth re-heat entrance, the other end of the second methane rich liquid phase transfer lime is connected to the 11 re-heat entrance of First Heat Exchanger, the 11 re-heat outlet of First Heat Exchanger is connected to the SNG storage tank by the SNG line of pipes, and the 11 re-heat outlet is communicated with the 11 re-heat entrance;
The methane rich liquid phase outlet of described methane rectifier bottoms also is connected with one the 3rd methane rich liquid phase transfer lime, the 3rd methane rich liquid phase transfer lime is connected with the entrance of described liquid methane pump, described liquid methane pump outlet is connected to the 12 re-heat entrance of the second interchanger by the 4th methane rich liquid phase transfer lime, the 12 re-heat outlet of the second interchanger is connected to the 13 re-heat entrance of First Heat Exchanger by the 5th methane rich liquid phase transfer lime, the 12 re-heat outlet is communicated with the 12 re-heat entrance, and the 13 re-heat outlet of First Heat Exchanger is connected to gasification workshop section by the high-pressure gas transfer lime; The 13 re-heat outlet is communicated with the 13 re-heat entrance.
2. coke(oven)gas as claimed in claim 1 or LURGI stove/BGL producer gas ammonia combination preparing device processed, it is characterized in that, described methane rectifying tower cat head condenser is built in the described methane rectifying tower, and the 3rd gaseous phase outlet at described methane rectifying tower top connects with the hot junction outlet of methane rectifying tower cat head condenser.
3. coke(oven)gas as claimed in claim 1 or LURGI stove/BGL producer gas ammonia combination preparing device processed, it is characterized in that, also comprise a methane rectifying tower return tank, described methane rectifying tower cat head condenser is external outside methane rectifying tower cat head, and the hot junction outlet of described methane rectifying tower cat head condenser is connected with the entrance of methane rectifying tower return tank; Top at methane rectifying tower return tank is provided with the 7th gaseous phase outlet, and the bottom of methane rectifying tower return tank is provided with bypass outlet; Top at the methane rectifying tower is provided with reflux inlet, and the 7th gaseous phase outlet is connected with described the first exhaust pipe by the 7th gas-phase transport pipe; The bypass outlet of methane rectifying tower return tank bottom is connected by the reflux inlet of return line with the methane rectifier.
4. coke(oven)gas as claimed in claim 1 or LURGI stove/BGL producer gas ammonia combination preparing device processed is characterized in that, is provided with liquid nitrogen in the bottom of described C0 rich solution tank and replenishes mouth, and this liquid nitrogen replenishes mouth and replenishes pipe connecting fluid nitrogenous source by liquid nitrogen.
5. coke(oven)gas as claimed in claim 1 or LURGI stove/BGL producer gas ammonia combination preparing device processed, it is characterized in that, described third high presses the other end of nitrogen transfer lime not tell two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime are told in the 3rd condensation outlet of described the 3rd interchanger, be connected to the first re-heat entrance of described the 3rd interchanger on the first high pressure low temperature liquid nitrogen transfer lime the other end behind series connection one reducing valve, the second high pressure low temperature liquid nitrogen transfer lime the other end is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top; The first liquid-phase outlet is connected with the second re-heat entrance of described the 3rd interchanger by the first liquid phase transfer lime, the second re-heat outlet of the 3rd interchanger is connected with the second liquid phase entrance of methane rectifier by the second liquid phase transfer lime, and the second re-heat entrance is communicated with the second re-heat outlet; The 3rd re-heat outlet of the 3rd interchanger is communicated with the first re-heat entrance and the 3rd re-heat entrance, and the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe.
6. coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, comprise First Heat Exchanger, the second interchanger, the 3rd interchanger and nitrogen wash column, it is characterized in that, also comprise methane rectifying tower, methane rectifying tower cat head condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, carbon monoxide rich solution tank, liquid methane pump;
Divide the first high pressure nitrogen transfer lime that is connected to be connected with the first condensation entrance of described First Heat Exchanger with sky, one end of the second high pressure nitrogen transfer lime is connected with the first condensation of described First Heat Exchanger outlet, the first condensation entrance is communicated with the first condensation outlet, the other end of the second high pressure nitrogen transfer lime is connected with the second condensation entrance of described the second interchanger, third high presses an end of nitrogen transfer lime to be connected with the second condensation outlet of described the second interchanger, the second condensation entrance is communicated with the second condensation outlet, third high presses the other end of nitrogen transfer lime to be divided into two strands, and one third high presses the nitrogen transfer lime to be connected with the 3rd condensation entrance of described the 3rd interchanger; The 3rd condensation outlet of described the 3rd interchanger connects an end of the first high pressure low temperature liquid nitrogen transfer lime, and the 3rd condensation entrance is communicated with the 3rd condensation outlet, and the first high pressure low temperature liquid nitrogen transfer lime is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top;
The the first raw hydrogen transfer lime that is connected with molecular sieve is connected with the 4th condensation entrance of described the second interchanger, one end of the second raw hydrogen transfer lime is connected with the 4th condensation of described the second interchanger outlet, the 4th condensation entrance is communicated with the 4th condensation outlet, the other end of the second raw hydrogen transfer lime is connected with the 5th condensation entrance of described the 3rd interchanger, one end of the 3rd raw hydrogen transfer lime is connected with the 5th condensation of described the 3rd interchanger outlet, the 5th condensation entrance is communicated with the 5th condensation outlet, and the other end of the 3rd raw hydrogen transfer lime is connected with the raw hydrogen entrance on described unstripped gas flash tank top;
Described unstripped gas flash tank cat head is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of the unstripped gas flash tank tower, the first gaseous phase outlet is connected with the first gas phase entrance of nitrogen wash column bottom by the first gas-phase transport pipe, and the first liquid-phase outlet is connected with the second liquid phase entrance of methane rectifier by the first liquid phase transfer lime;
Be provided with at the top of nitrogen wash column and remove CO, Ar, CH 4The second gaseous phase outlet behind the impurity, the bottom of nitrogen wash column is provided with liquid rich CO cut outlet, the second gaseous phase outlet connects by the 3rd re-heat entrance of the second gas-phase transport Guan Yudi three interchanger, the 3rd re-heat outlet of the 3rd interchanger is communicated with the first re-heat entrance and the 3rd re-heat entrance, the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe, and the second gas-phase transport pipe presses the nitrogen transfer lime to be connected with another burst third high; The 4th re-heat outlet of the second interchanger is the first virgin gas transfer lime, the first virgin gas transfer lime is divided into two strands, wherein the other end of one the first virgin gas transfer lime is connected with the entrance of described methane rectifying tower tower bottom reboiler, the outlet of methane rectifying tower tower bottom reboiler connects low-temperature rectisol workshop section entrance by the second virgin gas transfer lime, and the re-heat outlet of low-temperature rectisol workshop section connects the 3rd virgin gas transfer lime; The other end of another strand the first virgin gas transfer lime connects the 6th re-heat entrance of First Heat Exchanger, and the 6th re-heat outlet of First Heat Exchanger connects ammonia synthesis workshop section by the bright letter shoot of the "four news" (new ideas, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Described the 3rd virgin gas transfer lime is connected with the bright letter shoot of the described "four news" (new ideas;
The liquid rich CO cut outlet of nitrogen wash column bottom is connected to the entrance of carbon monoxide rich solution tank by the rich CO cut of liquid state transfer lime, the top of carbon monoxide rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of carbon monoxide rich solution tank is provided with the 3rd liquid-phase outlet; The 3rd liquid-phase outlet is connected with the cold junction entrance of methane rectifying tower cat head condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower cat head condenser connects an end of the 5th gas-phase transport pipe, the 4th gaseous phase outlet connects an end of the 4th gas-phase transport pipe, the other end of the other end of the 4th gas-phase transport pipe and the 5th gas-phase transport pipe and connect after the 7th re-heat entrance by the 6th gas-phase transport Guan Yudi three interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat of the 3rd interchanger outlet, and the 7th re-heat entrance is communicated with the 7th re-heat outlet; The other end of the first exhaust pipe is connected with the 8th re-heat entrance of the second interchanger, one end of the second exhaust pipe is connected with the 8th re-heat of the second interchanger outlet, the 8th re-heat outlet is communicated with the 8th re-heat entrance, the other end of the second exhaust pipe is connected with the 9th re-heat entrance of First Heat Exchanger, one end of the 3rd exhaust pipe is connected with the 9th re-heat of First Heat Exchanger outlet, the 9th re-heat outlet is communicated with another termination gas ductwork of the 3rd exhaust pipe with the 9th re-heat entrance;
The top of described methane rectifying tower is provided with the 3rd gaseous phase outlet, the bottom of methane rectifying tower is provided with the outlet of methane rich liquid phase, the 3rd gaseous phase outlet is connected with the hot junction entrance of described methane rectifying tower cat head condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower cat head condenser is connected with the 4th liquid phase transfer lime;
The methane rich liquid phase outlet of methane rectifier bottoms is connected to the entrance of liquid methane pump by the 6th methane rich liquid phase transfer lime, the liquid methane pump outlet connects the 7th methane rich liquid phase transfer lime and the 8th methane rich liquid phase transfer lime, be provided with variable valve at the 7th methane rich liquid phase transfer lime and the 8th methane rich liquid phase transfer lime, the other end of the 7th methane rich liquid phase transfer lime is connected with the 14 condensation entrance of the 3rd interchanger, and the 14 condensation outlet of the 3rd interchanger connects the LNG storage tank by the LNG transfer lime; The 8th methane rich liquid phase transfer lime is connected with the 12 re-heat entrance of the second interchanger, the 12 re-heat outlet of the second interchanger is connected to the 13 re-heat entrance of First Heat Exchanger by the 5th methane rich liquid phase transfer lime, the 12 re-heat outlet is communicated with the 12 re-heat entrance, and the 13 re-heat outlet of First Heat Exchanger is connected to gasification workshop section by the high-pressure gas transfer lime; The 13 re-heat outlet is communicated with the 13 re-heat entrance.
7. coke(oven)gas as claimed in claim 6 or LURGI stove/BGL producer gas ammonia combination preparing device processed, it is characterized in that, described methane rectifying tower cat head condenser is built in the described methane rectifying tower, and the 3rd gaseous phase outlet at described methane rectifying tower top connects with the hot junction outlet of methane rectifying tower cat head condenser.
8. coke(oven)gas as claimed in claim 6 or LURGI stove/BGL producer gas ammonia combination preparing device processed, it is characterized in that, also comprise a methane rectifying tower return tank, described methane rectifying tower cat head condenser is external outside methane rectifying tower cat head, and the hot junction outlet of described methane rectifying tower cat head condenser is connected with the entrance of methane rectifying tower return tank; Top at methane rectifying tower return tank is provided with the 7th gaseous phase outlet, and the bottom of methane rectifying tower return tank is provided with bypass outlet; Top at the methane rectifying tower is provided with reflux inlet, and the 7th gaseous phase outlet is connected with described the first exhaust pipe by the 7th gas-phase transport pipe; The bypass outlet of methane rectifying tower return tank bottom is connected by the reflux inlet of return line with the methane rectifier.
9. coke(oven)gas as claimed in claim 6 or LURGI stove/BGL producer gas ammonia combination preparing device processed is characterized in that, connects a Claude cycle refrigeration system between described First Heat Exchanger and the second interchanger; This Claude cycle refrigeration system is by a decompressor, one compressor and a water cooler form, wherein the entrance of compressor is connected with the first cold loop exit of First Heat Exchanger, the outlet of compressor is connected with the hot junction entrance of water cooler, the hot junction outlet of water cooler is connected with the second cold loop head of First Heat Exchanger, the second cold loop exit of First Heat Exchanger is connected with the 3rd cold loop head of the second interchanger, the second cold loop exit is communicated with the second cold loop head, the 3rd cold loop exit of the second interchanger is connected with the entrance of decompressor, the outlet of decompressor is connected with the 4th cold loop head of the second interchanger, the 4th cold loop exit of the second interchanger is connected with the first cold loop head of First Heat Exchanger, the 4th cold loop exit is communicated with the 4th cold loop head, and the first cold loop head is communicated with the first cold loop exit.
10. coke(oven)gas as claimed in claim 6 or LURGI stove/BGL producer gas ammonia combination preparing device processed, it is characterized in that, described third high presses the other end of nitrogen transfer lime not tell two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime are told in the 3rd condensation outlet of described the 3rd interchanger, be connected to the first re-heat entrance of described the 3rd interchanger on the first high pressure low temperature liquid nitrogen transfer lime the other end behind series connection one reducing valve, the second high pressure low temperature liquid nitrogen transfer lime the other end is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top; The first liquid-phase outlet is connected with the second re-heat entrance of described the 3rd interchanger by the first liquid phase transfer lime, the second re-heat outlet of the 3rd interchanger is connected with the second liquid phase entrance of methane rectifier by the second liquid phase transfer lime, and the second re-heat entrance is communicated with the second re-heat outlet; The 3rd re-heat outlet of the 3rd interchanger is communicated with the first re-heat entrance and the 3rd re-heat entrance, and the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe.
11. coke(oven)gas or LURGI stove/BGL producer gas ammonia combination preparing device processed, comprise First Heat Exchanger, the second interchanger, the 3rd interchanger and nitrogen wash column, it is characterized in that, also comprise methane rectifying tower, methane rectifying tower cat head condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, carbon monoxide rich solution tank;
Divide the first high pressure nitrogen transfer lime that is connected to be connected with the first condensation entrance of described First Heat Exchanger with sky, one end of the second high pressure nitrogen transfer lime is connected with the first condensation of described First Heat Exchanger outlet, the first condensation entrance is communicated with the first condensation outlet, the other end of the second high pressure nitrogen transfer lime is connected with the second condensation entrance of described the second interchanger, third high presses an end of nitrogen transfer lime to be connected with the second condensation outlet of described the second interchanger, the second condensation entrance is communicated with the second condensation outlet, third high presses the other end of nitrogen transfer lime to be divided into two strands, and one third high presses the nitrogen transfer lime to be connected with the 3rd condensation entrance of described the 3rd interchanger; The 3rd condensation outlet of described the 3rd interchanger connects an end of the first high pressure low temperature liquid nitrogen transfer lime, and the 3rd condensation entrance is communicated with the 3rd condensation outlet, and the first high pressure low temperature liquid nitrogen transfer lime is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top;
The the first raw hydrogen transfer lime that is connected with molecular sieve is connected with the 4th condensation entrance of described the second interchanger, one end of the second raw hydrogen transfer lime is connected with the 4th condensation of described the second interchanger outlet, the 4th condensation entrance is communicated with the 4th condensation outlet, the other end of the second raw hydrogen transfer lime is connected with the 5th condensation entrance of described the 3rd interchanger, one end of the 3rd raw hydrogen transfer lime is connected with the 5th condensation of described the 3rd interchanger outlet, the 5th condensation entrance is communicated with the 5th condensation outlet, and the other end of the 3rd raw hydrogen transfer lime is connected with the raw hydrogen entrance on described unstripped gas flash tank top;
Described unstripped gas flash tank cat head is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of the unstripped gas flash tank tower, the first gaseous phase outlet is connected with the first gas phase entrance of nitrogen wash column bottom by the first gas-phase transport pipe, and the first liquid-phase outlet is connected with the second liquid phase entrance of methane rectifier by the first liquid phase transfer lime;
Be provided with at the top of nitrogen wash column and remove CO, Ar, CH 4The second gaseous phase outlet behind the impurity, the bottom of nitrogen wash column is provided with liquid rich CO cut outlet, the second gaseous phase outlet connects by the 3rd re-heat entrance of the second gas-phase transport Guan Yudi three interchanger, the 3rd re-heat outlet of the 3rd interchanger is communicated with the first re-heat entrance and the 3rd re-heat entrance, the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe, and the second gas-phase transport pipe presses the nitrogen transfer lime to be connected with another burst third high; The 4th re-heat outlet of the second interchanger is the first virgin gas transfer lime, the first virgin gas transfer lime is divided into two strands, wherein the other end of one the first virgin gas transfer lime is connected with the entrance of described methane rectifying tower tower bottom reboiler, the outlet of methane rectifying tower tower bottom reboiler connects low-temperature rectisol workshop section entrance by the second virgin gas transfer lime, and the re-heat outlet of low-temperature rectisol workshop section connects the 3rd virgin gas transfer lime; The other end of another strand the first virgin gas transfer lime connects the 6th re-heat entrance of First Heat Exchanger, and the 6th re-heat outlet of First Heat Exchanger connects ammonia synthesis workshop section by the bright letter shoot of the "four news" (new ideas, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Described the 3rd virgin gas transfer lime is connected the rear ammonia synthetic fresh gas that forms with the bright letter shoot of the described "four news" (new ideas;
The liquid rich CO cut outlet of nitrogen wash column bottom is connected to the entrance of carbon monoxide rich solution tank by the rich CO cut of liquid state transfer lime, the top of carbon monoxide rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of carbon monoxide rich solution tank is provided with the 3rd liquid-phase outlet; The 3rd liquid-phase outlet is connected with the cold junction entrance of methane rectifying tower cat head condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower cat head condenser connects an end of the 5th gas-phase transport pipe, the 4th gaseous phase outlet connects an end of the 4th gas-phase transport pipe, the other end of the other end of the 4th gas-phase transport pipe and the 5th gas-phase transport pipe and connect after the 7th re-heat entrance by the 6th gas-phase transport Guan Yudi three interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat of the 3rd interchanger outlet, and the 7th re-heat entrance is communicated with the 7th re-heat outlet; The other end of the first exhaust pipe is connected with the 8th re-heat entrance of the second interchanger, one end of the second exhaust pipe is connected with the 8th re-heat of the second interchanger outlet, the 8th re-heat outlet is communicated with the 8th re-heat entrance, the other end of the second exhaust pipe is connected with the 9th re-heat entrance of First Heat Exchanger, one end of the 3rd exhaust pipe is connected with the 9th re-heat of First Heat Exchanger outlet, the 9th re-heat outlet is communicated with another termination gas ductwork of the 3rd exhaust pipe with the 9th re-heat entrance;
The top of described methane rectifying tower is provided with the 3rd gaseous phase outlet, the bottom of methane rectifying tower is provided with the outlet of methane rich liquid phase, the 3rd gaseous phase outlet is connected with the hot junction entrance of described methane rectifying tower cat head condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower cat head condenser is connected with the 4th liquid phase transfer lime;
The methane rich liquid phase outlet of methane rectifier bottoms also is connected to the first methane rich liquid phase transfer lime and the tenth methane rich liquid phase transfer lime, be provided with variable valve at the first methane rich liquid phase transfer lime, the other end of the first methane rich liquid phase transfer lime is connected with the tenth re-heat entrance of the second interchanger, one end of the second methane rich liquid phase transfer lime is connected to the tenth re-heat outlet of the second interchanger, the tenth re-heat outlet is communicated with the tenth re-heat entrance, the other end of the second methane rich liquid phase transfer lime is connected to the 11 re-heat entrance of First Heat Exchanger, the 11 re-heat outlet of First Heat Exchanger is connected to the SNG storage tank by the SNG line of pipes, and the 11 re-heat outlet is communicated with the 11 re-heat entrance; The tenth methane rich liquid phase transfer lime is connected to the entrance of liquid methane pump, the liquid methane pump outlet also connects the 7th methane rich liquid phase transfer lime and the 8th methane rich liquid phase transfer lime, be provided with variable valve at the 7th methane rich liquid phase transfer lime and the 8th methane rich liquid phase transfer lime, the other end of the 7th methane rich liquid phase transfer lime is connected with the 14 re-heat entrance of the 3rd interchanger, and the 14 re-heat outlet of the 3rd interchanger connects the LNG storage tank by the LNG transfer lime; The 8th methane rich liquid phase transfer lime is connected with the 12 re-heat entrance of the second interchanger, the 12 re-heat outlet of the second interchanger is connected to the 13 re-heat entrance of First Heat Exchanger by the 5th methane rich liquid phase transfer lime, the 12 re-heat outlet is communicated with the 12 re-heat entrance, and the 13 re-heat outlet of First Heat Exchanger is connected to gasification workshop section by the high-pressure gas transfer lime; The 13 re-heat outlet is communicated with the 13 re-heat entrance.
12. coke(oven)gas as claimed in claim 11 or LURGI stove/BGL producer gas ammonia combination preparing device processed, it is characterized in that, described methane rectifying tower cat head condenser is built in the described methane rectifying tower, and the 3rd gaseous phase outlet at described methane rectifying tower top connects with the hot junction outlet of methane rectifying tower cat head condenser.
13. coke(oven)gas as claimed in claim 11 or LURGI stove/BGL producer gas ammonia combination preparing device processed, it is characterized in that, also comprise a methane rectifying tower return tank, described methane rectifying tower cat head condenser is external outside methane rectifying tower cat head, and the hot junction outlet of described methane rectifying tower cat head condenser is connected with the entrance of methane rectifying tower return tank; Top at methane rectifying tower return tank is provided with the 7th gaseous phase outlet, and the bottom of methane rectifying tower return tank is provided with bypass outlet; Top at the methane rectifying tower is provided with reflux inlet, and the 7th gaseous phase outlet is connected with described the first exhaust pipe by the 7th gas-phase transport pipe; The bypass outlet of methane rectifying tower return tank bottom is connected by the reflux inlet of return line with the methane rectifier.
14. coke(oven)gas as claimed in claim 11 or LURGI stove/BGL producer gas ammonia combination preparing device processed is characterized in that, connect a Claude cycle refrigeration system between described First Heat Exchanger and the second interchanger; This Claude cycle refrigeration system is by a decompressor, one compressor and a water cooler form, wherein the entrance of compressor is connected with the first cold loop exit of First Heat Exchanger, the outlet of the first decompressor is connected with the hot junction entrance of water cooler, the hot junction outlet of water cooler is connected with the second cold loop head of First Heat Exchanger, the second cold loop exit of First Heat Exchanger is connected with the 3rd cold loop head of the second interchanger, the second cold loop exit is communicated with the second cold loop head, the 3rd cold loop exit of the second interchanger is connected with the entrance of the second decompressor, the outlet of the second decompressor is connected with the 4th cold loop head of the second interchanger, the 4th cold loop exit of the second interchanger is connected with the first cold loop head of First Heat Exchanger, the 4th cold loop exit is communicated with the 4th cold loop head, and the first cold loop head is communicated with the first cold loop exit.
15. coke(oven)gas as claimed in claim 11 or LURGI stove/BGL producer gas ammonia combination preparing device processed is characterized in that, are provided with liquid nitrogen in the bottom of described carbon monoxide rich solution tank and replenish mouth, this liquid nitrogen replenishes mouth and replenishes pipe connecting fluid nitrogenous source by liquid nitrogen.
16. coke(oven)gas as claimed in claim 11 or LURGI stove/BGL producer gas ammonia combination preparing device processed, it is characterized in that, described third high presses the other end of nitrogen transfer lime not tell two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime are told in the 3rd condensation outlet of described the 3rd interchanger, be connected to the first re-heat entrance of described the 3rd interchanger on the first high pressure low temperature liquid nitrogen transfer lime the other end behind series connection one reducing valve, the second high pressure low temperature liquid nitrogen transfer lime the other end is connected to the high pressure low temperature liquid nitrogen entrance on described nitrogen wash column top; The first liquid-phase outlet is connected with the second re-heat entrance of described the 3rd interchanger by the first liquid phase transfer lime, the second re-heat outlet of the 3rd interchanger is connected with the second liquid phase entrance of methane rectifier by the second liquid phase transfer lime, and the second re-heat entrance is communicated with the second re-heat outlet; The 3rd re-heat outlet of the 3rd interchanger is communicated with the first re-heat entrance and the 3rd re-heat entrance, and the 3rd re-heat outlet of the 3rd interchanger is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport pipe.
CN2012203434776U 2012-07-13 2012-07-13 Coke-oven gas or LURGI furnace/British Gas-Lurgi furnace coal gasification ammonia-production co-production device Withdrawn - After Issue CN202864908U (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103121662A (en) * 2012-07-13 2013-05-29 上海国际化建工程咨询公司 Method and device for purifying ammonia synthesis virgin gas and co-generating SNG (synthetic natural gas) or/and LNG (liquefied natural gas) via liquid nitrogen washing

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103121662A (en) * 2012-07-13 2013-05-29 上海国际化建工程咨询公司 Method and device for purifying ammonia synthesis virgin gas and co-generating SNG (synthetic natural gas) or/and LNG (liquefied natural gas) via liquid nitrogen washing
CN103121662B (en) * 2012-07-13 2016-03-02 上海国际化建工程咨询公司 Liquid nitrogen washing purification ammonia synthetic fresh gas co-production SNG processed is or/and the method for LNG and device

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