CN103121662A - 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 - Google Patents

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 Download PDF

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CN103121662A
CN103121662A CN2012102454349A CN201210245434A CN103121662A CN 103121662 A CN103121662 A CN 103121662A CN 2012102454349 A CN2012102454349 A CN 2012102454349A CN 201210245434 A CN201210245434 A CN 201210245434A CN 103121662 A CN103121662 A CN 103121662A
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gas
outlet
interchanger
heat
entrance
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CN103121662B (en
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章华勇
顾鹤燕
杨震东
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Shanghai International Engineering Consulting Co
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SHANGHAI INTERNATIONAL CONSTRUCTION ENGINEERING CONSULTING CO LTD
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • 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
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    • 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
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • 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
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    • F25J2200/00—Processes or apparatus using separation by rectification
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    • 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
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    • 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
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    • 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
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    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/14—Coke-ovens gas
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    • 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
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    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
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    • 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
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    • 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
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/32—Hydrogen storage

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  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
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Abstract

The invention discloses a method and a device for purifying ammonia synthesis virgin gas and co-generating SNG (synthetic natural gas) or/and LNG (liquefied natural gas) via liquid nitrogen washing, wherein by the addition of a methane rectification tower and a liquid methane pump in a conventional liquid nitrogen washing device, and a reasonable line configuration, a methane-rich fraction can be re-heated and then used as a city gas and output; the methane-rich fraction can also be cyclically refrigerated via Claude and used for producing the LNG product; simultaneously, a product adjustment can be performed on SNG and LNG according to different used loads.

Description

Liquid nitrogen washing purification ammonia synthetic fresh gas processed coproduction SNG are or/and the method for LNG and device
Technical field
The present invention relates to coke(oven)gas or LURGI stove/BGL stove and produce the synthetic ammonia technical gas field of purification in the coal chemical technology of synthetic ammonia, be particularly related to and a kind ofly take coal as raw material, utilize LURGI stove or BGL stove for the gasification mode, or take the raw hydrogen (hydrogen, carbon monoxide, nitrogen, methane, argon) that coke(oven)gas is raw material, purify the preparation ammonia synthetic fresh gas, produce synthetic ammonia, and the method and apparatus of by-product SNG, LNG and high-pressure gas product.The present invention is exactly mainly for adopting coke(oven)gas or LURGI stove/BGL stove to produce the coal chemical technology of synthetic ammonia.
Background technology
Due to 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 coking industry is rationally taken full advantage of, coke(oven)gas is also in a large number for chemical industry.
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, need to remove through the liquid nitrogen washing operation gas that the rare gas element such as methane and carbon monoxide etc. are harmful to catalyzer in the synthetic ammonia process of producing product, could meet the requirement that synthetic ammonia process is produced.For the methane rich cut separated, domestic each coal chemical industry enterprises is taked different processing modes.
One, referring to Fig. 1, raw gas/coke(oven)gas is delivered to after low-temperature rectisol, liquid nitrogen washing operation are removed the gas that the rare gas element such as methane and carbon monoxide etc. are harmful to catalyzer and is delivered to synthetic ammonia process after CO conversion, and Zhongdao synthesis procedure is produced ammonia.The low-temperature rectisol operation is got back to again after the liquid nitrogen washing operation directly being delivered to methane conversion, non-sulfur-resisting transformation workshop section after methane rich cut re-heat out by some enterprises.
The method exists following obviously not enough: 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, invest highly, 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, due to the difference of flow process configuration, all existence current employing or that applied for a patent are not enough as follows: 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, due 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 developed 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 use gas in town gas, considers the difficulty of town gas accumulating, produces the LNG natural gas liquids to adjust the product mix simultaneously, and reply is moving with wave is imperative.
From current 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 the difference due to the 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 as how lower energy consumption.
Summary of the invention
One of technical problem to be solved by this invention is for existing coke(oven)gas or LURGI stove/BGL furnace gas and produces low temperature liquid nitrogen in ammonia synthesis process and wash the existing problem of technique and provide a kind of liquid nitrogen washing to purify the method for preparation ammonia synthetic fresh gas coproduction SNG, the method 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 meet the requirement of ammonia synthesis process to virgin gas, by the reasonable disposition on stream to the methane rectifying tower, realize that under the condition of less energy-consumption the production of high yield meets SNG and the high-pressure gas of relevant criterion.
Two of technical problem to be solved by this invention is to wash the existing problem of technique and provide liquid nitrogen washing to purify the method for preparation ammonia synthetic fresh gas coproduction LNG for low temperature liquid nitrogen in existing coke(oven)gas or LURGI stove/BGL furnace gas production ammonia synthesis process, the method 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 meet the requirement of ammonia synthesis process to virgin gas, by the reasonable disposition on stream to the methane rectifying tower, 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 by this invention is to wash the existing problem of technique and provide liquid nitrogen washing to purify the method for preparation ammonia synthetic fresh gas coproduction SNG and LNG for low temperature liquid nitrogen in existing coke(oven)gas or LURGI stove/BGL furnace gas production ammonia synthesis process, the method 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 meet the requirement of ammonia synthesis process to virgin gas, by the reasonable disposition on stream to the methane rectifying tower, 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, the impact in Various Seasonal demands different from the period, fluctuation produced to solve downstream user, realize the steady running of whole synthetic ammonia installation simultaneously.
Four of technical problem to be solved by this invention is to provide and realizes that above-mentioned liquid nitrogen washing purifies the device of preparation ammonia synthetic fresh gas coproduction SNG.
Five of technical problem to be solved by this invention is to provide and realizes that above-mentioned liquid nitrogen washing purifies the device of preparation ammonia synthetic fresh gas coproduction LNG.
Six of technical problem to be solved by this invention is to provide and realizes that above-mentioned liquid nitrogen washing purifies the device of preparation ammonia synthetic fresh gas coproduction SNG and LNG.
Purify the method for preparation ammonia synthetic fresh gas coproduction SNG as the liquid nitrogen washing of first aspect present invention, it is characterized in that, send in the raw material flash tank after the second interchanger and the 3rd interchanger are cooled to-180～-190 ℃ from the raw hydrogen of molecular sieve and carry out flash distillation and obtain the first gas phase and the first liquid phase; The first gas phase after flash distillation enters into the nitrogen wash column bottom by the tank deck outflow of raw material flash tank; High pressure nitrogen be divided into two strands after First Heat Exchanger, the second interchanger are cooling in the middle of high pressure nitrogens, it is-180～-190 ℃ of high pressure low temperature liquid nitrogens that one middle high pressure nitrogen is sent into the cooling rear formation temperature of the 3rd interchanger, this high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column, removes CO, Ar, CH in described the first gas phase 4impurity, form and remove CO, Ar, CH 4the second gas phase after impurity and liquid rich CO cut;
Remove CO, Ar, CH 4the second gas phase after impurity is flowed out by the nitrogen wash column tower top; The second gas phase flowed out by the nitrogen wash column tower top with high pressure nitrogen in the middle of another strand, mixes regulate hydrogen nitrogen compare to 2.9～3.1 and after the second interchanger re-heat formation temperature be-50～-65 ℃ of first virgin gases;
The first virgin gas is divided into two strands, one first virgin gas obtains the second virgin gas that temperature is-55～-70 ℃ after delivering to the reboiler cooling at the bottom of the methane rectifying tower, and it is 25～35 ℃ of the 3rd virgin gas that described the second virgin gas is delivered to low-temperature rectisol workshop section re-heat to temperature; Another burst first virgin gas again after the First Heat Exchanger re-heat formation temperature be 25～35 ℃ of the 4th virgin gas, the 4th virgin gas is mixed formation ammonia synthetic fresh gas afterwards and is delivered to synthetic ammonia workshop section with the 3rd virgin gas;
The first liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank, after constant enthalpy is decompressed to 0.25～0.35MPa, by the top of described methane rectifying tower, is delivered in the methane rectifying tower and is carried out methane rectifying; Methane rich liquid phase after methane rectifying is gone out by the tower bottom flow of described methane rectifying tower, after the second interchanger, First Heat Exchanger re-heat to 35 ℃, delivers to the SNG storage tank; The 3rd gas phase after methane rectifying is flowed out by the tower top of described methane rectifying tower;
The rich CO cut of described liquid state is gone out by the tower bottom flow of nitrogen wash column, tower bottom flow by nitrogen wash column goes out liquid rich CO cut after constant enthalpy is decompressed to 0.25～0.35MPa, deliver in CO rich solution tank and carry out flash distillation, the 3rd liquid phase that after flash distillation, formation temperature is-180～-195 ℃ and the 4th gas phase, the 3rd liquid phase is gone out to deliver to the condenser cold junction of described methane rectifying tower tower top by CO rich solution tank tank underflow, carry out heat exchange with the 3rd gas phase that tower top by described methane rectifying tower flows out in described condenser, the 3rd liquid phase forms the 5th gas phase after self heating up in described condenser and gasifying, the 5th gas phase is mixed and is formed the 6th gas phase of-150～-160 ℃ by the 3rd interchanger re-heat with the 4th gas phase flowed out by CO rich solution tank tank deck, the 3rd gas phase flowed out by the tower top of described methane rectifying tower forms the 4th liquid phase and delivers to the return tank of methane rectifying tower tower top and carry out the gas-liquid flash distillation in described condenser after condensation, the 7th gas phase after the gas-liquid flash distillation is mixed with described the 6th gas phase by the second interchanger, First Heat Exchanger re-heat to 25～35 ℃ formation tail gas and sent to gas ductwork, the 5th liquid phase after the gas-liquid flash distillation is as the methane rectifying column top return.
In the method for coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purification preparation ammonia synthetic fresh gas coproduction SNG, the methane rich liquid phase gone out by the tower bottom flow of described methane rectifying tower is divided into two strands, and one methane-rich liquid continues to deliver to the SNG storage tank mutually after the second interchanger, First Heat Exchanger re-heat to 25～35 ℃; Another strand of methane-rich liquid forms the high-pressure gas that required pressure, temperature are 25～35 ℃ and sends to battery limit (BL) by the supercharging of liquid methane pump and after the second interchanger, First Heat Exchanger re-heat.
In the method for coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purification preparation ammonia synthetic fresh gas coproduction SNG, the 5th liquid-phase reflux methane rectifying tower tower top total reflux after described gas-liquid flash distillation.
Above-mentioned coke(oven)gas or LURGI stove/BGL producer gas liquid nitrogen washing purify in the method for preparation ammonia synthetic fresh gas coproduction SNG, and its low temperature cold measures reasonable utilization, the self cooling balance of whole device, in normal productive process without out-of-bounds inputting cold.But, consider the fluctuation of production process, the drawback that may exist in operation, the method is supplemented liquid nitrogen, the cold deficiency that may cause to eliminate above-mentioned reason in described CO rich solution tank.
The first liquid phase after described flash distillation is gone out by the tank underflow of raw material flash tank, carry out re-heat by the 3rd interchanger after constant enthalpy is decompressed to 0.25～0.35MPa, re-heat to the second liquid phase of-150～-160 ℃ is delivered in the methane rectifying tower and is carried out methane rectifying by the top of described methane rectifying tower; Described high pressure nitrogen formation temperature after First Heat Exchanger, the second interchanger and the 3rd interchanger are cooling is-180～-190 ℃ of high pressure low temperature liquid nitrogens, this high pressure low temperature liquid nitrogen is divided into two strands, and one high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column; Another strand of high pressure low temperature liquid nitrogen return in the 3rd interchanger with the second gas phase flowed out by the nitrogen wash column tower top in the 3rd interchanger, mixes regulate hydrogen nitrogen compare to 2.9～3.1 and after the 3rd interchanger, the second interchanger re-heat formation temperature be-50～-65 ℃ of first virgin gases.
Purify the method for preparation ammonia synthetic fresh gas coproduction LNG as the liquid nitrogen washing of second aspect present invention, it is characterized in that, send in the raw material flash tank after the second interchanger and the 3rd interchanger are cooled to-180～-190 ℃ from the raw hydrogen of molecular sieve and carry out flash distillation and obtain the first gas phase and the first liquid phase; The first gas phase after flash distillation enters into the nitrogen wash column bottom by the tank deck outflow of raw material flash tank; High pressure nitrogen in the middle of high pressure nitrogen forms after First Heat Exchanger, the second interchanger are cooling, this centre high pressure nitrogen is divided into two strands, it is-180～-190 ℃ of high pressure low temperature liquid nitrogens that one middle high pressure nitrogen is sent into the cooling rear formation temperature of the 3rd interchanger, this high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column, removes CO, Ar, CH in described the first gas phase 4impurity, form and remove CO, Ar, CH 4the second gas phase after impurity and liquid rich CO cut;
Remove CO, Ar, CH 4the second gas phase after impurity is flowed out by the nitrogen wash column tower top; The second gas phase flowed out by the nitrogen wash column tower top is mixed and is regulated hydrogen nitrogen ratio to 2.9～3.1 with high pressure nitrogen in the middle of another strand, and formation temperature is-45～-65 ℃ of first virgin gases after the second interchanger re-heat;
The first virgin gas is divided into two strands, one first virgin gas obtains the second virgin gas that temperature is-50～-70 ℃ after delivering to the reboiler cooling at the bottom of the methane rectifying tower, and it is 25～35 ℃ of the 3rd virgin gas that described the second virgin gas is delivered to low-temperature rectisol workshop section re-heat to temperature; Another burst first virgin gas again after the First Heat Exchanger re-heat formation temperature be 25～35 ℃ of the 4th virgin gas, the 4th virgin gas is mixed formation ammonia synthetic fresh gas afterwards and is delivered to synthetic ammonia workshop section with the 3rd virgin gas;
The first liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank, after constant enthalpy is decompressed to 0.25～0.35MPa, by the top of described methane rectifying tower, is delivered in the methane rectifying tower and is carried out methane rectifying; Methane rich liquid phase after methane rectifying is gone out by the tower bottom flow of described methane rectifying tower, after the supercharging of liquid methane pump, is divided into two strands, one methane rich liquid phase.
The high-pressure gas that the required pressure of formation, temperature are 25～35 ℃ after the second interchanger, First Heat Exchanger re-heat is sent to battery limit (BL); Another strand of methane-rich liquid crossed and is as cold as-162 ℃ and delivers to the LNG storage tank by the 3rd interchanger; The 3rd gas phase after methane rectifying is flowed out by the tower top of described methane rectifying tower;
The rich CO cut of described liquid state is gone out by the tower bottom flow of nitrogen wash column, tower bottom flow by nitrogen wash column goes out liquid rich CO cut after constant enthalpy is decompressed to 0.25～0.35MPa, deliver in CO rich solution tank and carry out flash distillation, the 3rd liquid phase that after flash distillation, formation temperature is-180～-195 ℃ and the 4th gas phase, the 3rd liquid phase is gone out to deliver to the condenser cold junction of described methane rectifying tower tower top by CO rich solution tank tank underflow, carry out heat exchange with the 3rd gas phase that tower top by described methane rectifying tower flows out in described condenser, the 3rd liquid phase forms the 5th gas phase after self heating up in described condenser and gasifying, the 5th gas phase is mixed and is formed the 6th gas phase of-150～-160 ℃ by the 3rd interchanger re-heat with the 4th gas phase flowed out by CO rich solution tank tank deck, the 3rd gas phase flowed out by the tower top of described methane rectifying tower forms the 4th liquid phase and delivers to the return tank of methane rectifying tower tower top and carry out the gas-liquid flash distillation in described condenser after condensation, the 7th gas phase after the gas-liquid flash distillation is mixed with described the 6th gas phase by the second interchanger, First Heat Exchanger re-heat to 25～35 ℃ formation tail gas and sent to gas ductwork, the 5th liquid phase after the gas-liquid flash distillation is as the methane rectifying column top return.
In liquid nitrogen washing, purify in the method for preparation ammonia purified gas coproduction LNG, due to the product of only producing the LNG specification, the low temperature cold of system can not meet the requirement of self, so set up a Claude cycle refrigeration system between described First Heat Exchanger and the second interchanger, for system provides cold, produce the LNG product.
Purify in the method for preparation ammonia synthetic fresh gas coproduction LNG the 5th liquid-phase reflux methane rectifying tower tower top total reflux after described gas-liquid flash distillation in liquid nitrogen washing.
The first liquid phase after described flash distillation is gone out by the tank underflow of raw material flash tank, carry out re-heat by the 3rd interchanger after constant enthalpy is decompressed to 0.25～0.35MPa, re-heat to the second liquid phase of-150～-160 ℃ is delivered in the methane rectifying tower and is carried out methane rectifying by the top of described methane rectifying tower; Described high pressure nitrogen formation temperature after First Heat Exchanger, the second interchanger and the 3rd interchanger are cooling is-180～-190 ℃ of high pressure low temperature liquid nitrogens, this high pressure low temperature liquid nitrogen is divided into two strands, and one high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column; Another strand of high pressure low temperature liquid nitrogen return in the 3rd interchanger with the second gas phase flowed out by the nitrogen wash column tower top in the 3rd interchanger, mixes regulate hydrogen nitrogen compare to 2.9～3.1 and after the 3rd interchanger, the second interchanger re-heat formation temperature be-50～-65 ℃ of first virgin gases.
Purify the method for preparation ammonia synthetic fresh gas coproduction SNG and LNG as the liquid nitrogen washing of third aspect present invention, it is characterized in that, send in the raw material flash tank after the second interchanger and the 3rd interchanger are cooled to-180～-190 ℃ from the raw hydrogen of molecular sieve and carry out flash distillation and obtain the first gas phase and the first liquid phase; The first gas phase after flash distillation enters into the nitrogen wash column bottom by the tank deck outflow of raw material flash tank; High pressure nitrogen in the middle of high pressure nitrogen forms after First Heat Exchanger, the second interchanger are cooling, this centre high pressure nitrogen is divided into two strands, it is-180～-190 ℃ of high pressure low temperature liquid nitrogens that one middle high pressure nitrogen is sent into the cooling rear formation temperature of the 3rd interchanger, this high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column, removes CO, Ar, CH in described the first gas phase 4impurity, form and remove CO, Ar, CH 4the second gas phase after impurity and liquid rich CO cut;
Remove CO, Ar, CH 4the second gas phase after impurity is flowed out by the nitrogen wash column tower top; The second gas phase flowed out by the nitrogen wash column tower top is mixed and is regulated hydrogen nitrogen ratio to 2.9～3.1 with high pressure nitrogen in the middle of another strand, and formation temperature is-45～-65 ℃ of first virgin gases after the second interchanger re-heat;
The first virgin gas is divided into two strands, one first virgin gas obtains the second virgin gas that temperature is-50～-70 ℃ after delivering to the reboiler cooling at the bottom of the methane rectifying tower, and it is 25～35 ℃ of the 3rd virgin gas that described the second virgin gas is delivered to low-temperature rectisol workshop section re-heat to temperature; Another burst first virgin gas again after the First Heat Exchanger re-heat formation temperature be 25～35 ℃ of the 4th virgin gas, the 4th virgin gas is mixed formation ammonia synthetic fresh gas afterwards and is delivered to synthetic ammonia workshop section with the 3rd virgin gas;
The first liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank, after constant enthalpy is decompressed to 0.25～0.35MPa, by the top of described methane rectifying tower, is delivered in the methane rectifying tower and is carried out methane rectifying; Methane rich liquid phase after methane rectifying is gone out by the tower bottom flow of described methane rectifying tower, go out the methane rich liquid phase by the tower bottom flow of described methane rectifying tower and be divided into two strands, wherein one methane rich liquid phase is delivered to the SNG storage tank after the second interchanger, First Heat Exchanger re-heat to 35 ℃; Another strand of methane-rich liquid is divided into two thighs after the supercharging of liquid methane pump, and thigh methane rich liquid phase forms the high-pressure gas that required pressure, temperature are 25～35 ℃ and sends to battery limit (BL) after the second interchanger, First Heat Exchanger re-heat; Another thigh methane-rich liquid is crossed and is as cold as-162 ℃ and delivers to the LNG storage tank by the 3rd interchanger; The 3rd gas phase after methane rectifying is flowed out by the tower top of described methane rectifying tower;
The rich CO cut of described liquid state is gone out by the tower bottom flow of nitrogen wash column, tower bottom flow by nitrogen wash column goes out liquid rich CO cut after constant enthalpy is decompressed to 0.25～0.35MPa, deliver in CO rich solution tank and carry out flash distillation, the 3rd liquid phase that after flash distillation, formation temperature is-180～-195 ℃ and the 4th gas phase, the 3rd liquid phase is gone out to deliver to the condenser cold junction of described methane rectifying tower tower top by CO rich solution tank tank underflow, carry out heat exchange with the 3rd gas phase that tower top by described methane rectifying tower flows out in described condenser, the 3rd liquid phase forms the 5th gas phase after self heating up in described condenser and gasifying, the 5th gas phase is mixed and is formed the 6th gas phase of-150～-160 ℃ by the 3rd interchanger re-heat with the 4th gas phase flowed out by CO rich solution tank tank deck, the 3rd gas phase flowed out by the tower top of described methane rectifying tower forms the 4th liquid phase and delivers to the return tank of methane rectifying tower tower top and carry out the gas-liquid flash distillation in described condenser after condensation, the 7th gas phase after the gas-liquid flash distillation is mixed with described the 6th gas phase by the second interchanger, First Heat Exchanger re-heat to 25～35 ℃ formation tail gas and sent to gas ductwork, the 5th liquid phase after the gas-liquid flash distillation is as the methane rectifying column top return.
In liquid nitrogen washing, purify in the method for preparation ammonia synthetic fresh gas coproduction SNG and LNG, due to the product that can produce SNG and two kinds of specifications of LNG simultaneously, the low temperature cold of system can not meet the requirement of self, so set up a Claude cycle refrigeration system or/and supplement liquid nitrogen in described CO rich solution tank between described First Heat Exchanger and the second interchanger, for system provides cold, produce the LNG/SNG product.
Purify in the method for preparation ammonia purified gas coproduction SNG and LNG the 5th liquid-phase reflux methane rectifying tower tower top total reflux after described gas-liquid flash distillation in liquid nitrogen washing.
The first liquid phase after described flash distillation is gone out by the tank underflow of raw material flash tank, carry out re-heat by the 3rd interchanger after constant enthalpy is decompressed to 0.25～0.35MPa, re-heat to the second liquid phase of-150～-160 ℃ is delivered in the methane rectifying tower and is carried out methane rectifying by the top of described methane rectifying tower; Described high pressure nitrogen formation temperature after First Heat Exchanger, the second interchanger and the 3rd interchanger are cooling is-180～-190 ℃ of high pressure low temperature liquid nitrogens, this high pressure low temperature liquid nitrogen is divided into two strands, and one high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column; Another strand of high pressure low temperature liquid nitrogen return in the 3rd interchanger with the second gas phase flowed out by the nitrogen wash column tower top in the 3rd interchanger, mixes regulate hydrogen nitrogen compare to 2.9～3.1 and after the 3rd interchanger, the second interchanger re-heat formation temperature be-50～-65 ℃ of first virgin gases.
Purify the device of preparation ammonia synthetic fresh gas coproduction SNG as the liquid nitrogen washing of fourth aspect present invention, 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 tower top condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, C0 rich solution tank, liquid methane pump;
With sky, divide the first high pressure nitrogen transfer lime be connected to be connected with the first condensation entrance of described First Heat Exchanger, one end of the second high pressure nitrogen transfer lime is connected with the first condensation outlet of described First Heat Exchanger, 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, 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 be 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 outlet of described the second interchanger, 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 outlet of described the 3rd interchanger, the 5th condensation entrance is communicated with the 5th condensation outlet, 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 tower top is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of 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 and remove CO, Ar, CH at the top of nitrogen wash column 4the second gaseous phase outlet after 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 Yu tri-interchanger, the 3rd re-heat outlet the 3rd re-heat entrance of the 3rd interchanger is communicated with, the 3rd re-heat outlet of the 3rd interchanger is taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport, and the second gas-phase transport is taken over another burst of third high and pressed the nitrogen transfer lime to be connected; 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 is carried to take over by the second virgin gas and is connected low-temperature rectisol workshop section entrance, and the re-heat outlet of low-temperature rectisol workshop section is the 3rd virgin gas; 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 is carried to take over by the 4th virgin gas and connected ammonia synthesis workshop section, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Low-temperature rectisol workshop section also carries to take over by the 3rd virgin gas transfer lime and described the 4th virgin gas and is connected the rear ammonia synthetic fresh gas that forms;
The rich CO cut outlet of the liquid state of nitrogen wash column bottom is connected to the entrance of C0 rich solution tank by the rich CO cut of liquid state transfer lime, the top of C0 rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of C0 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 tower top condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower tower top 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 Yu tri-interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat outlet of the 3rd interchanger, 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 outlet of the second interchanger, 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 outlet of First Heat Exchanger, the 9th re-heat outlet is communicated with the 9th re-heat entrance, another termination gas ductwork of the 3rd exhaust pipe;
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 tower top condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower tower top 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, 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 liquid nitrogen washing, purify in the device of preparation ammonia synthetic fresh gas coproduction SNG, described methane rectifying tower tower top condenser is built in 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 tower top condenser.
In liquid nitrogen washing, purify in the device of preparation ammonia synthetic fresh gas coproduction SNG, also comprise a methane rectifying tower return tank, described methane rectifying tower tower top condenser is external outside methane rectifying tower tower top, and the hot junction outlet of described methane rectifying tower tower top condenser is connected with the entrance of methane rectifying tower return tank; Be provided with the 7th gaseous phase outlet at the top of methane rectifying tower return tank, 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 with the reflux inlet of methane rectifier by return line.
Be provided with liquid nitrogen in the bottom of described C0 rich solution tank and supplement mouth, this liquid nitrogen supplements mouth and supplements pipe connecting fluid nitrogenous source by liquid nitrogen.
Described third high presses the other end of nitrogen transfer lime not separate two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the 3rd condensation outlet of described the 3rd interchanger separates the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime, on the first high pressure low temperature liquid nitrogen transfer lime after series connection one reducing valve the other end be connected to the first re-heat entrance of described the 3rd interchanger, 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 carried to take over by second liquid phase and is connected with the second liquid phase entrance of methane rectifier, 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 taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport.
Purify the device of preparation ammonia synthetic fresh gas coproduction LNG as the liquid nitrogen washing of fifth aspect present invention, 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 tower top condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, C0 rich solution tank, liquid methane pump;
With sky, divide the first high pressure nitrogen transfer lime be connected to be connected with the first condensation entrance of described First Heat Exchanger, one end of the second high pressure nitrogen transfer lime is connected with the first condensation outlet of described First Heat Exchanger, 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, 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 be 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 outlet of described the second interchanger, 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 outlet of described the 3rd interchanger, the 5th condensation entrance is communicated with the 5th condensation outlet, 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 tower top is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of 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 and remove CO, Ar, CH at the top of nitrogen wash column 4the second gaseous phase outlet after 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 Yu tri-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 the 3rd re-heat entrance of the 3rd interchanger is communicated with, the 3rd re-heat outlet of the 3rd interchanger is taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport, and the second gas-phase transport is taken over another burst of third high and pressed the nitrogen transfer lime to be connected; 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 is carried to take over by the second virgin gas and is connected low-temperature rectisol workshop section entrance, and the re-heat outlet of low-temperature rectisol workshop section is the 3rd virgin gas; 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 is carried to take over by the 4th virgin gas and connected ammonia synthesis workshop section, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Low-temperature rectisol workshop section also carries to take over by the 3rd virgin gas transfer lime and described the 4th virgin gas and is connected the rear ammonia synthetic fresh gas that forms;
The rich CO cut outlet of the liquid state of nitrogen wash column bottom is connected to the entrance of C0 rich solution tank by the rich CO cut of liquid state transfer lime, the top of C0 rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of C0 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 tower top condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower tower top 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 Yu tri-interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat outlet of the 3rd interchanger, 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 outlet of the second interchanger, 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 outlet of First Heat Exchanger, the 9th re-heat outlet is communicated with the 9th re-heat entrance, another termination gas ductwork of the 3rd exhaust pipe;
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 tower top condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower tower top 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 on 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 liquid nitrogen washing, purify in the device of preparation ammonia synthetic fresh gas coproduction LNG, described methane rectifying tower tower top condenser is built in 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 tower top condenser.
In liquid nitrogen washing, purify in the device of preparation ammonia synthetic fresh gas coproduction LNG, also comprise a methane rectifying tower return tank, described methane rectifying tower tower top condenser is external outside methane rectifying tower tower top, and the hot junction outlet of described methane rectifying tower tower top condenser is connected with the entrance of methane rectifying tower return tank; Be provided with the 7th gaseous phase outlet at the top of methane rectifying tower return tank, 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 with the reflux inlet of methane rectifier by return line.
Purify in the device of preparation ammonia synthetic fresh gas coproduction LNG in liquid nitrogen washing, 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 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, 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 separate two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the 3rd condensation outlet of described the 3rd interchanger separates the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime, on the first high pressure low temperature liquid nitrogen transfer lime after series connection one reducing valve the other end be connected to the first re-heat entrance of described the 3rd interchanger, 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 carried to take over by second liquid phase and is connected with the second liquid phase entrance of methane rectifier, 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 taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport.
Purify the device of preparation ammonia synthetic fresh gas coproduction SNG and LNG as the liquid nitrogen washing of sixth aspect present invention, 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 tower top condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, C0 rich solution tank;
With sky, divide the first high pressure nitrogen transfer lime be connected to be connected with the first condensation entrance of described First Heat Exchanger, one end of the second high pressure nitrogen transfer lime is connected with the first condensation outlet of described First Heat Exchanger, 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, 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 be 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 outlet of described the second interchanger, 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 outlet of described the 3rd interchanger, the 5th condensation entrance is communicated with the 5th condensation outlet, 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 tower top is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of 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 and remove CO, Ar, CH at the top of nitrogen wash column 4the second gaseous phase outlet after 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 Yu tri-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 the 3rd re-heat entrance of the 3rd interchanger is communicated with, the 3rd re-heat outlet of the 3rd interchanger is taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport, and the second gas-phase transport is taken over another burst of third high and pressed the nitrogen transfer lime to be connected; 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 is carried to take over by the second virgin gas and is connected low-temperature rectisol workshop section entrance, and the re-heat outlet of low-temperature rectisol workshop section is the 3rd virgin gas; 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 is carried to take over by the 4th virgin gas and connected ammonia synthesis workshop section, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Low-temperature rectisol workshop section also carries to take over by the 3rd virgin gas transfer lime and described the 4th virgin gas and is connected the rear ammonia synthetic fresh gas that forms;
The rich CO cut outlet of the liquid state of nitrogen wash column bottom is connected to the entrance of C0 rich solution tank by the rich CO cut of liquid state transfer lime, the top of C0 rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of C0 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 tower top condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower tower top 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 Yu tri-interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat outlet of the 3rd interchanger, 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 outlet of the second interchanger, 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 outlet of First Heat Exchanger, the 9th re-heat outlet is communicated with the 9th re-heat entrance, another termination gas ductwork of the 3rd exhaust pipe;
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 tower top condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower tower top condenser is connected with the 4th liquid phase transfer lime;
The methane rich liquid phase of methane rectifier bottoms exports and 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 on 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, 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 on 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 liquid nitrogen washing, purify in the device of preparation ammonia synthetic fresh gas coproduction SNG and LNG, described methane rectifying tower tower top condenser is built in 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 tower top condenser.
In liquid nitrogen washing, purify in the device of preparation ammonia synthetic fresh gas coproduction SNG and LNG, also comprise a methane rectifying tower return tank, described methane rectifying tower tower top condenser is external outside methane rectifying tower tower top, and the hot junction outlet of described methane rectifying tower tower top condenser is connected with the entrance of methane rectifying tower return tank; Be provided with the 7th gaseous phase outlet at the top of methane rectifying tower return tank, 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 with the reflux inlet of methane rectifier by return line.
Purify in the device of preparation ammonia synthetic fresh gas coproduction SNG and LNG in liquid nitrogen washing, 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, the first cold loop head is communicated with the first cold loop exit.
In the device of above-mentioned liquid nitrogen washing purification preparation ammonia synthetic fresh gas coproduction SNG and LNG, be provided with liquid nitrogen in the bottom of described C0 rich solution tank and supplement mouth, this liquid nitrogen supplements mouth and supplements pipe connecting fluid nitrogenous source by liquid nitrogen.
Described third high presses the other end of nitrogen transfer lime not separate two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the 3rd condensation outlet of described the 3rd interchanger separates the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime, on the first high pressure low temperature liquid nitrogen transfer lime after series connection one reducing valve the other end be connected to the first re-heat entrance of described the 3rd interchanger, 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 carried to take over by second liquid phase and is connected with the second liquid phase entrance of methane rectifier, 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 taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport.
Owing to having adopted technical scheme as above, the present invention arranges methane rectifying tower, methane rectifying tower tower top 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, after the liquid phase constant enthalpy decompression from the unstripped gas flash tank, return after the 3rd interchanger reclaims cold and enter into the methane rectifying tower, can greatly lower like this consumption of low temperature cold, reduce energy consumption.
Methane rectifying tower of the present invention 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 tower top condenser comes from the liquid phase of CO 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 the methane in unstripped gas, reach the purpose of product concentrate simultaneously, make product meet national standard.
Methane rectifying tower tower top condenser of the present invention, tower bottom reboiler are loaded adjustable, to adapt to different operating modes and to meet the finished product requirement.
Cancel methane rectifying column top return tank thereby methane rectifying tower tower top condenser of the present invention can be built directly in the methane rectifying tower, reduce facility investment.
The present invention is directed to coke(oven)gas or take coal as raw material, utilize LURGI stove or BGL stove for the gasification mode, purify 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.
The accompanying drawing explanation
Fig. 1 delivers to after the CO conversion for existing raw gas/coke(oven)gas after low-temperature rectisol, liquid nitrogen washing operation are removed the gas that the rare gas element such as methane and carbon monoxide etc. are harmful to catalyzer and delivers to synthetic ammonia process, 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 liquid nitrogen washing of the present invention purifies preparation ammonia synthetic fresh gas coproduction SNG and/or LNG.
Fig. 4 is a kind of device schema that liquid nitrogen washing of the present invention purifies preparation ammonia synthetic fresh gas coproduction SNG.
Fig. 5 is the another kind of device schema that liquid nitrogen washing of the present invention purifies preparation ammonia synthetic fresh gas coproduction SNG.
Fig. 6 is a kind of device schema that liquid nitrogen washing of the present invention purifies preparation ammonia synthetic fresh gas coproduction LNG.
Fig. 7 is the another kind of device schema that liquid nitrogen washing of the present invention purifies preparation ammonia synthetic fresh gas coproduction LNG.
Fig. 8 is a kind of device schema that liquid nitrogen washing of the present invention purifies preparation ammonia synthetic fresh gas coproduction SNG and LNG.
Fig. 9 is the another kind of device schema that liquid nitrogen washing of the present invention purifies preparation ammonia synthetic fresh gas coproduction SNG and LNG.
Figure 10 is that methane rectifying tower tower top condenser of the present invention is built in the structural representation in described methane rectifying tower.
Embodiment
Referring to Fig. 3, technical process of the present invention is that raw gas/coke(oven)gas is through CO conversion, low-temperature rectisol, the synthetic virgin gas of liquid nitrogen washing coproduction SNG and/or LNG and high-pressure gas.Specific embodiment is as follows:
Embodiment 1
Referring to Fig. 4, Fig. 4 has provided liquid nitrogen washing and has purified a kind of device schema of preparing ammonia synthetic fresh gas coproduction SNG.
This 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 tower top 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.
With sky, divide the nitrogen compressor 1100 be connected to be connected with the condensation entrance 120 of interchanger 100 by high pressure nitrogen transfer lime 10, 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; The condensation outlet 321 of interchanger 300 separates high pressure low temperature liquid nitrogen transfer lime 20,21, and condensation entrance 320 is communicated with condensation outlet 321.
On high pressure low temperature liquid nitrogen transfer lime 21, after series connection one reducing valve 22, the other end is connected to the re-heat entrance 330 of interchanger 300, 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 be 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 tower tops are provided with gaseous phase outlet 820, be provided with liquid-phase outlet 830 at the bottom of tower, gaseous phase outlet 820 is connected with the gas phase entrance 420 of nitrogen wash column 400 bottoms by gas-phase transport pipe 40, 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 carries adapter 43 to be connected with the liquid phase entrance 510 on methane rectifying tower 500 tops by liquid phase, and re-heat entrance 340 is communicated with re-heat outlet 341.Be serially connected with constant enthalpy reducing valve 42 on liquid phase transfer lime 41.
Be provided with and remove CO, Ar, CH at the tower top of nitrogen wash column 400 4gaseous phase outlet 430 after impurity, be provided with liquid rich CO cut outlet 440 at the bottom of 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 outlet 351 of interchanger 300 is taken over 51 by gas-phase transport and is connected with the re-heat entrance 240 of interchanger 200, the re-heat outlet 241 of interchanger 200 separates virgin gas transfer lime 60, 61, the other end of virgin gas transfer lime 60 is connected with the entrance of methane rectifying tower 500 tower bottom reboilers 700, the outlet of methane rectifying tower tower bottom reboiler 700 is carried and is taken over 62 connection low-temperature rectisol workshop sections 1200 by virgin gas.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 is carried and taken over 63 connection ammonia synthesis workshop sections 1300 by virgin gas, and re-heat entrance 140 is communicated with re-heat outlet 141; Low-temperature rectisol workshop section 1200 also carries adapter 63 to be connected by virgin gas return tube 64 and virgin gas.
The rich CO cut outlet 440 of liquid state 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 bottom is provided with liquid-phase outlet 930; Be serially connected with constant enthalpy reducing valve 79 on liquid rich CO cut transfer lime 70.
Liquid-phase outlet 930 is connected with the cold junction entrance of methane rectifying tower tower top condenser 600 by liquid phase transfer lime 72, the cold side outlet of methane rectifying tower tower top 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 by gas-phase transport arm 75, with the re-heat entrance 360 of interchanger 300, be connected, 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 re-heat entrance 130, another termination gas ductwork 1400 of exhaust pipe 78.
The tower top 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 tower, methane rectifying tower tower top condenser 600 is as for outside methane rectifying tower 500, gaseous phase outlet 520 is connected with the hot junction entrance of methane rectifying tower tower top condenser 600 by gas-phase transport pipe 80, and the hot junction outlet of methane rectifying tower tower top 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 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 outlet 151 of interchanger 100 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 outlet 161 of interchanger 100 is connected to gasification workshop section 1700 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 supplement mouth 940, this liquid nitrogen supplements mouth 940 and supplements pipe 941 connecting fluid nitrogenous sources by liquid nitrogen.
The technical process of this embodiment is as follows: enter interchanger 200 from the raw hydrogen of molecular sieve by raw hydrogen transfer lime 30 interior cooling, and then it is interior further cooling to enter interchanger 300 by raw hydrogen transfer lime 31, by interchanger 300, raw hydrogen temperature out is-180～-190 ℃.The raw hydrogen of this temperature is sent into the interior flash distillation of raw material flash tank 800 by raw hydrogen transfer lime 32, and the gas phase after flash distillation is flowed out by the tank deck of raw material flash tank 800, by gas-phase transport pipe 40, enters into nitrogen wash column 400 bottoms.
The medium pressure nitrogen gas divided from sky forms high pressure nitrogen after the nitrogen compressor compression, it is interior cooling that high pressure nitrogen enters interchanger 100 by high pressure nitrogen transfer lime 10, send into interchanger 200 through the cooled high pressure nitrogen of interchanger 100 by high pressure nitrogen transfer lime 11 interior further cooling, send into by high pressure nitrogen transfer lime 12 through interchanger 200 further cooled high pressure nitrogen that in interchanger 300, a step is cooling again, final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.
By interchanger 300, high pressure low temperature liquid nitrogen out is 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 interior flash distillation of nitrogen wash column 400 the gas phase counter current contact, remove CO, Ar, CH in the gas phase after flash distillation 4impurity, form and remove CO, Ar, CH 4gas phase after impurity and liquid rich CO cut.Remove CO, Ar, CH 4gas phase after impurity meets the ammonia synthesis catalyst requirement.
Remove CO, Ar, CH 4gas phase after impurity is flowed out by nitrogen wash column 400 tower tops, by gas-phase transport pipe 50, sends into interchanger 300 re-heats; Another strand returns to 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 re-heat 4gas phase after impurity forms virgin gas after mixing, and the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.
Virgin gas is sent into the interior further re-heat of interchanger 200 by virgin gas transfer lime 51 again becomes the virgin gas that temperature is-45～-65 ℃; This virgin gas is divided into two strands, one obtains the virgin gas that temperature be-50～-70 ℃ after delivering to reboiler 700 coolings at the bottom of the methane rectifying tower by virgin gas transfer lime 60, and then by virgin gas, carrying adapter 62 to deliver to low-temperature rectisol workshop section 1200 re-heats to temperature is 25～35 ℃ of virgin gases; Another burst of virgin gas is sent into interchanger 100 re-heats by virgin gas transfer lime 61, formation temperature is 25～35 ℃ of virgin gases, and the virgin gas that this virgin gas is brought by virgin gas return tube 64 with low-temperature rectisol workshop section 1200 carries adapter 63 to send into synthetic ammonia workshop section 1300 by virgin gas after mixing.
Liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank 800, after constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, turn back in interchanger 300 and carry out re-heat by liquid phase transfer lime 41, re-heat carries adapter 43 to be entered in methane rectifying tower 500 by methane rectifying tower 500 tower tops by liquid phase 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 rectifying is flowed out by the tower top of methane rectifying tower 500.The methane rich liquid phase volumetric molar concentration 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 while normally moving, the methane rich liquid phase gone out by the tower bottom flow of methane rectifying tower 500 is divided into two strands, after one sends into the re-heat of the interior recovery cold of interchanger 200 by methane rich liquid phase transfer lime 92, then send into the re-heat of the interior recovery cold of interchanger 100 by methane rich liquid phase transfer lime 93 and deliver to SNG storage tank 1600 to 25～35 ℃ of SNG delivery temperatures.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 the further re-heat of interchanger 100 by methane rich liquid phase transfer lime 97 again and form high-pressure gas, by high-pressure gas transfer lime 98, be connected to gasification workshop section 1700.
The rich CO cut of the liquid state 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 CO rich solution tank 900 and carry out flash distillation by the rich CO cut of liquid state transfer lime 70, the liquid and gas that after flash distillation, formation temperature is-180～-195 ℃, liquid phase is gone out by CO rich solution tank 900 tank underflows, deliver to condenser 600 cold junctions of methane rectifying tower 500 tower tops by liquid phase transfer lime 72, for it, after being provided, cold returns, after the gas phase of bringing by gas-phase transport pipe 73 is mixed, send into after cold is reclaimed in the interior re-heat of interchanger 300 and send by exhaust pipe 76 by gas-phase transport arm 75, with send into the interior further re-heat of interchanger 200 after the gas phase by after the 90 methane rectifying tower return tank 1500 gas-liquid flash distillations of gas-phase transport pipe is mixed and reclaim cold, sending in interchanger 100 a step re-heat again by exhaust pipe 77 again reclaims after 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 tower top outflow rectifying of methane rectifying tower 500 by gas-phase transport pipe 80, after with entering condenser 600, the interior liquid phase of-180～-195 ℃ is carried 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, in normal productive process without out-of-bounds inputting cold.But, consider the fluctuation of production process, the drawback that may exist in operation, the method is supplemented pipe 941 to the interior supplementary liquid nitrogen of CO rich solution tank 900, the cold deficiency that may cause to eliminate above-mentioned reason by liquid nitrogen.
Embodiment 2
Referring to Fig. 5, Fig. 5 has provided liquid nitrogen washing and has purified the another kind of device schema of preparing ammonia synthetic fresh gas coproduction SNG.
The difference of this embodiment and embodiment 1 is exactly: the other end of high pressure nitrogen transfer lime 12 separates two strands, one high pressure nitrogen transfer lime 12a is connected with the condensation entrance 320 of interchanger 300, and another gang of high pressure nitrogen transfer lime 12b directly is connected with virgin gas transfer lime 51.321 of the condensation outlets of interchanger 300 separate high pressure low temperature liquid nitrogen transfer lime 20, do not separate 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 conveying adapter 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 the load of interchanger 200,300 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 thermal source of the high pressure nitrogen of the second heat exchanger exit as the methane rectifying tower, and the cold of methane rectifying tower tower top condenser still comes from the liquid phase of CO rich solution tank.
The process distinction of this embodiment and embodiment is: through the further cooled high pressure nitrogen of interchanger 200, be divided into two strands, one is sent into by high pressure nitrogen transfer lime 12a, and in interchanger 300, a step is cooling again, and final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.Remove CO, Ar, CH 4gas phase after impurity is flowed out by nitrogen wash column 400 tower tops, by gas-phase transport pipe 50, sends into interchanger 300 re-heats, after re-heat, removes CO, Ar, CH 4form virgin gas after another strand of high pressure nitrogen that gas phase after impurity is brought with high pressure nitrogen transfer lime 12b mixes, the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.Liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank 800, after constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, do not need to turn back in interchanger 300 and carry out re-heat by liquid phase transfer lime 41, but directly by liquid phase, carry adapter 43 to enter in methane rectifying tower 500 and made with extra care by methane rectifying tower 500 tower tops.
Embodiment 3:
Referring to Fig. 6, Fig. 6 has provided liquid nitrogen washing and has purified a kind of device schema of preparing ammonia synthetic fresh gas coproduction LNG.
This 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 tower top 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.
With sky, divide the nitrogen compressor 1100 be connected to be connected with the condensation entrance 120 of interchanger 100 by high pressure nitrogen transfer lime 10, 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; The condensation outlet 321 of interchanger 300 separates high pressure low temperature liquid nitrogen transfer lime 20,21, and condensation entrance 320 is communicated with condensation outlet 321.
On high pressure low temperature liquid nitrogen transfer lime 21, after series connection one reducing valve 22, the other end is connected to the re-heat entrance 330 of interchanger 300, 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 be 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 tower tops are provided with gaseous phase outlet 820, be provided with liquid-phase outlet 830 at the bottom of tower, gaseous phase outlet 820 is connected with the gas phase entrance 420 of nitrogen wash column 400 bottoms by gas-phase transport pipe 40, 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 carries adapter 43 to be connected with the liquid phase entrance 510 on methane rectifying tower 500 tops by liquid phase, and re-heat entrance 340 is communicated with re-heat outlet 341.Be serially connected with constant enthalpy reducing valve 42 on liquid phase transfer lime 41.
Be provided with and remove CO, Ar, CH at the tower top of nitrogen wash column 400 4gaseous phase outlet 430 after impurity, be provided with liquid rich CO cut outlet 440 at the bottom of 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 outlet 351 of interchanger 300 is taken over 51 by gas-phase transport and is connected with the re-heat entrance 240 of interchanger 200, the re-heat outlet 241 of interchanger 200 separates virgin gas transfer lime 60, 61, the other end of virgin gas transfer lime 60 is connected with the entrance of methane rectifying tower 500 tower bottom reboilers 700, the outlet of methane rectifying tower tower bottom reboiler 700 is carried and is taken over 62 connection low-temperature rectisol workshop sections 1200 by virgin gas.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 is carried and taken over 63 connection ammonia synthesis workshop sections 1300 by virgin gas, and re-heat entrance 140 is communicated with re-heat outlet 141; Low-temperature rectisol workshop section 1200 also carries adapter 63 to be connected by virgin gas return tube 64 and virgin gas.
The rich CO cut outlet 440 of liquid state 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 bottom is provided with liquid-phase outlet 930; Be serially connected with constant enthalpy reducing valve 79 on liquid rich CO cut transfer lime 70.
Liquid-phase outlet 930 is connected with the cold junction entrance of methane rectifying tower tower top condenser 600 by liquid phase transfer lime 72, the cold side outlet of methane rectifying tower tower top 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 by gas-phase transport arm 75, with the re-heat entrance 360 of interchanger 300, be connected, 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 re-heat entrance 130, another termination gas ductwork 1400 of exhaust pipe 78.
The tower top 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 tower, methane rectifying tower tower top condenser 600 is as for outside methane rectifying tower 500, gaseous phase outlet 520 is connected with the hot junction entrance of methane rectifying tower tower top condenser 600 by gas-phase transport pipe 80, and the hot junction outlet of methane rectifying tower tower top 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 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 on 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 outlet 161 of interchanger 100 is connected to gasification workshop section 1700 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 2, this 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, cold loop head 170 is communicated with cold loop exit 171.
The technical process of this embodiment is as follows: enter interchanger 200 from the raw hydrogen of molecular sieve by raw hydrogen transfer lime 30 interior cooling, and then it is interior further cooling to enter interchanger 300 by raw hydrogen transfer lime 31, by interchanger 300, raw hydrogen temperature out is-180～-190 ℃.The raw hydrogen of this temperature is sent into the interior flash distillation of raw material flash tank 800 by raw hydrogen transfer lime 32, and the gas phase after flash distillation is flowed out by the tank deck of raw material flash tank 800, by gas-phase transport pipe 40, enters into nitrogen wash column 400 bottoms.
The medium pressure nitrogen gas divided from sky forms high pressure nitrogen after nitrogen compressor 1100 compressions, it is interior cooling that high pressure nitrogen enters interchanger 100 by high pressure nitrogen transfer lime 10, send into interchanger 200 through the cooled high pressure nitrogen of interchanger 100 by high pressure nitrogen transfer lime 11 interior further cooling, send into by high pressure nitrogen transfer lime 12 through interchanger 200 further cooled high pressure nitrogen that in interchanger 300, a step is cooling again, final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.
By interchanger 300, high pressure low temperature liquid nitrogen out is 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 entered after the interior flash distillation of nitrogen wash column 400, remove CO, Ar, CH in the gas phase after flash distillation 4impurity, form and remove CO, Ar, CH 4gas phase after impurity and liquid rich CO cut.Remove CO, Ar, CH 4gas phase after impurity meets the ammonia synthesis catalyst requirement.
Remove CO, Ar, CH 4gas phase after impurity is flowed out by nitrogen wash column 400 tower tops, by gas-phase transport pipe 50, sends into interchanger 300 re-heats; Another strand returns to 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 re-heat 4gas phase after impurity forms virgin gas after mixing, and the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.
Virgin gas is sent into the interior further re-heat of interchanger 200 by virgin gas transfer lime 51 again becomes the virgin gas that temperature is-45～-65 ℃; This virgin gas is divided into two strands, one obtains the virgin gas that temperature be-50～-70 ℃ after delivering to reboiler 700 coolings at the bottom of the methane rectifying tower by virgin gas transfer lime 60, and then by virgin gas, carrying adapter 62 to deliver to low-temperature rectisol workshop section 1200 re-heats to temperature is 25～35 ℃ of virgin gases; Another burst of virgin gas is sent into interchanger 100 re-heats by virgin gas transfer lime 61, formation temperature is 25～35 ℃ of virgin gases, and the virgin gas that this virgin gas is brought by virgin gas return tube 64 with low-temperature rectisol workshop section 1200 carries adapter 63 to send into synthetic ammonia workshop section 1300 by virgin gas after mixing.
Liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank 800, after constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, turn back in interchanger 300 and carry out re-heat by liquid phase transfer lime 41, re-heat carries adapter 43 to be entered in methane rectifying tower 500 by methane rectifying tower 500 tower tops by liquid phase 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 rectifying is flowed out by the tower top of methane rectifying tower 500.The methane rich liquid phase volumetric molar concentration 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 while 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 after reducing valve 96c decompression, sending into interchanger 200 re-heats, after interchanger 200 re-heats, send into the further re-heat of interchanger 100 by methane rich liquid phase transfer lime 97 again and form high-pressure gas, by high-pressure gas transfer lime 98, be connected to gasification workshop section 1700.Another strand, by methane rich liquid phase transfer lime 96a and by sending into interchanger 300 condensations after variable valve 96d, delivered to LNG storage tank 1800 by LNG transfer lime 96b after interchanger 300 condenses to the temperature that meets LNG accumulating requirement.
The rich CO cut of the liquid state 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 CO rich solution tank 900 and carry out flash distillation by the rich CO cut of liquid state transfer lime 70, the liquid and gas that after flash distillation, formation temperature is-180～-195 ℃, liquid phase is gone out by CO rich solution tank 900 tank underflows, deliver to condenser 600 cold junctions of methane rectifying tower 500 tower tops by liquid phase transfer lime 72, for it, after being provided, cold returns, after the gas phase of bringing by gas-phase transport pipe 73 is mixed, send into after cold is reclaimed in the interior re-heat of interchanger 300 and send by exhaust pipe 76 by gas-phase transport arm 75, with send into the interior further re-heat of interchanger 200 after the gas phase by after the 90 methane rectifying tower return tank 1500 gas-liquid flash distillations of gas-phase transport pipe is mixed and reclaim cold, sending in interchanger 100 a step re-heat again by exhaust pipe 77 again reclaims after 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 tower top outflow rectifying of methane rectifying tower 500 by gas-phase transport pipe 80, after with entering condenser 600, the interior liquid phase of-180～-195 ℃ is carried 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 meet the requirement of self, so need to come into operation, the Claude circularly cooling is produced the LNG product for system provides cold, whole circulation loop adopts circulating water to take away heat, and without out-of-bounds inputting 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 liquid nitrogen washing and has purified the another kind of device schema of preparing ammonia synthetic fresh gas coproduction LNG.
The difference of this embodiment and embodiment 3 is exactly: the other end of high pressure nitrogen transfer lime 12 separates two strands, one high pressure nitrogen transfer lime 12a is connected with the condensation entrance 320 of interchanger 300, and another gang of high pressure nitrogen transfer lime 12b directly is connected with virgin gas transfer lime 51.321 of the condensation outlets of interchanger 300 separate high pressure low temperature liquid nitrogen transfer lime 20, do not separate 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 conveying adapter 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 the load of interchanger 200,300 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 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 thermal source of the high pressure nitrogen of the second heat exchanger exit as the methane rectifying tower, and the cold of methane rectifying tower tower top condenser still comes from the liquid phase of CO rich solution tank.
The process distinction of this embodiment and embodiment is: through the further cooled high pressure nitrogen of interchanger 200, be divided into two strands, one is sent into by high pressure nitrogen transfer lime 12a, and in interchanger 300, a step is cooling again, and final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.Remove CO, Ar, CH 4gas phase after impurity is flowed out by nitrogen wash column 400 tower tops, by gas-phase transport pipe 50, sends into interchanger 300 re-heats, after re-heat, removes CO, Ar, CH 4form virgin gas after another strand of high pressure nitrogen that gas phase after impurity is brought with high pressure nitrogen transfer lime 12b mixes, the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.Liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank 800, after constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, do not need to turn back in interchanger 300 and carry out re-heat by liquid phase transfer lime 41, but directly by liquid phase, carry adapter 43 to enter in methane rectifying tower 500 and made with extra care by methane rectifying tower 500 tower tops.
Embodiment 5:
Referring to Fig. 8, Fig. 8 has provided liquid nitrogen washing and has purified a kind of device schema of preparing ammonia synthetic fresh gas coproduction SNG and LNG.
This liquid nitrogen washing purifies the device of preparation ammonia synthetic fresh gas coproduction SNG and LNG, comprises interchanger 100,200,300, nitrogen wash column 400, methane rectifying tower 500, methane rectifying tower tower top 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.
With sky, divide the nitrogen compressor 1100 be connected to be connected with the condensation entrance 120 of interchanger 100 by high pressure nitrogen transfer lime 10, 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; The condensation outlet 321 of interchanger 300 separates high pressure low temperature liquid nitrogen transfer lime 20,21, and condensation entrance 320 is communicated with condensation outlet 321.
On high pressure low temperature liquid nitrogen transfer lime 21, after series connection one reducing valve 22, the other end is connected to the re-heat entrance 330 of interchanger 300, 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 be 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 tower tops are provided with gaseous phase outlet 820, be provided with liquid-phase outlet 830 at the bottom of tower, gaseous phase outlet 820 is connected with the gas phase entrance 420 of nitrogen wash column 400 bottoms by gas-phase transport pipe 40, 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 carries adapter 43 to be connected with the liquid phase entrance 510 on methane rectifying tower 500 tops by liquid phase, and re-heat entrance 340 is communicated with re-heat outlet 341.Be serially connected with constant enthalpy reducing valve 42 on liquid phase transfer lime 41.
Be provided with and remove CO, Ar, CH at the tower top of nitrogen wash column 400 4gaseous phase outlet 430 after impurity, be provided with liquid rich CO cut outlet 440 at the bottom of 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 outlet 351 of interchanger 300 is taken over 51 by gas-phase transport and is connected with the re-heat entrance 240 of interchanger 200, the re-heat outlet 241 of interchanger 200 separates virgin gas transfer lime 60, 61, the other end of virgin gas transfer lime 60 is connected with the entrance of methane rectifying tower 500 tower bottom reboilers 700, the outlet of methane rectifying tower tower bottom reboiler 700 is carried and is taken over 62 connection low-temperature rectisol workshop sections 1200 by virgin gas.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 is carried and taken over 63 connection ammonia synthesis workshop sections 1300 by virgin gas, and re-heat entrance 140 is communicated with re-heat outlet 141; Low-temperature rectisol workshop section 1200 also carries adapter 63 to be connected by virgin gas return tube 64 and virgin gas.
The rich CO cut outlet 440 of liquid state 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 bottom is provided with liquid-phase outlet 930; Be serially connected with constant enthalpy reducing valve 79 on liquid rich CO cut transfer lime 70.
Liquid-phase outlet 930 is connected with the cold junction entrance of methane rectifying tower tower top condenser 600 by liquid phase transfer lime 72, the cold side outlet of methane rectifying tower tower top 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 by gas-phase transport arm 75, with the re-heat entrance 360 of interchanger 300, be connected, 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 re-heat entrance 130, another termination gas ductwork 1400 of exhaust pipe 78.
The tower top 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 tower, methane rectifying tower tower top condenser 600 is as for outside methane rectifying tower 500, gaseous phase outlet 520 is connected with the hot junction entrance of methane rectifying tower tower top condenser 600 by gas-phase transport pipe 80, and the hot junction outlet of methane rectifying tower tower top 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 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 while 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 on 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 outlet 151 of interchanger 100 is connected to SNG storage tank 1600 by SNG line of pipes 94, 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 on methane rich liquid phase transfer lime 96,96a, SNG and LNG product structure are regulated and can be regulated by the flow be distributed on methane rich liquid phase transfer lime 92,92a.
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 outlet 161 of interchanger 100 is connected to gasification workshop section 1700 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 meet the requirement of self, so need to come into operation, the Claude circularly cooling provides cold or supplements pipe 941 by liquid nitrogen that to add liquid nitrogen in CO rich solution tank 940 be that system is supplemented cold for system, perhaps utilize the Claude circularly cooling simultaneously and supplement pipe 941 modes at CO rich solution tank 940 fluid infusion nitrogen by liquid nitrogen and produce the LNG product for the supplementary cold of system, connect a Claude cycle refrigeration system at interchanger 100,200, circulatory mediator is N for this reason 2, this 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, cold loop head 170 is communicated with cold loop exit 171.
The technical process of this embodiment is as follows: enter interchanger 200 from the raw hydrogen of molecular sieve by raw hydrogen transfer lime 30 interior cooling, and then it is interior further cooling to enter interchanger 300 by raw hydrogen transfer lime 31, by interchanger 300, raw hydrogen temperature out is-180～-190 ℃.The raw hydrogen of this temperature is sent into the interior flash distillation of raw material flash tank 800 by raw hydrogen transfer lime 32, and the gas phase after flash distillation is flowed out by the tank deck of raw material flash tank 800, by gas-phase transport pipe 40, enters into nitrogen wash column 400 bottoms.
The medium pressure nitrogen gas divided from sky forms high pressure nitrogen after nitrogen compressor 1100 compressions, it is interior cooling that high pressure nitrogen enters interchanger 100 by high pressure nitrogen transfer lime 10, send into interchanger 200 through the cooled high pressure nitrogen of interchanger 100 by high pressure nitrogen transfer lime 11 interior further cooling, send into by high pressure nitrogen transfer lime 12 through interchanger 200 further cooled high pressure nitrogen that in interchanger 300, a step is cooling again, final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.
By interchanger 300, high pressure low temperature liquid nitrogen out is 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 entered after the interior flash distillation of nitrogen wash column 400, remove CO, Ar, CH in the gas phase after flash distillation 4impurity, form and remove CO, Ar, CH 4gas phase after impurity and liquid rich CO cut.Remove CO, Ar, CH 4gas phase after impurity meets the ammonia synthesis catalyst requirement.
Remove CO, Ar, CH 4gas phase after impurity is flowed out by nitrogen wash column 400 tower tops, by gas-phase transport pipe 50, sends into interchanger 300 re-heats; Another strand returns to 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 re-heat 4gas phase after impurity forms virgin gas after mixing, and the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.
Virgin gas is sent into the interior further re-heat of interchanger 200 by virgin gas transfer lime 51 again becomes the virgin gas that temperature is-45～-65 ℃; This virgin gas is divided into two strands, one obtains the virgin gas that temperature be-50～-70 ℃ after delivering to reboiler 700 coolings at the bottom of the methane rectifying tower by virgin gas transfer lime 60, and then by virgin gas, carrying adapter 62 to deliver to low-temperature rectisol workshop section 1200 re-heats to temperature is 25～35 ℃ of virgin gases; Another burst of virgin gas is sent into interchanger 100 re-heats by virgin gas transfer lime 61, formation temperature is 25～35 ℃ of virgin gases, and the virgin gas that this virgin gas is brought by virgin gas return tube 64 with low-temperature rectisol workshop section 1200 carries adapter 63 to send into synthetic ammonia workshop section 1300 by virgin gas after mixing.
Liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank 830, after constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, turn back in interchanger 300 and carry out re-heat by liquid phase transfer lime 41, re-heat carries adapter 43 to be entered in methane rectifying tower 500 by methane rectifying tower 500 tower tops by liquid phase 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 rectifying is flowed out by the tower top of methane rectifying tower 500.The methane rich liquid phase volumetric molar concentration 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 while normally moving, the methane rich liquid phase gone out by the tower bottom flow of methane rectifying tower 500 is divided into two strands, after one sends into the re-heat of the interior recovery cold of interchanger 200 by methane rich liquid phase transfer lime 92, then send into the re-heat of the interior recovery cold of interchanger 200 by methane rich liquid phase transfer lime 93 and deliver to SNG storage tank 1600 by SNG transfer lime 94 to 35 ℃ of SNG delivery temperatures.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 after reducing valve 96c decompression, sending into interchanger 200 re-heats, after interchanger 200 re-heats, send into the further re-heat of interchanger 100 by methane rich liquid phase transfer lime 97 again and form high-pressure gas, by high-pressure gas transfer lime 98, be connected to gasification workshop section 1700.Another strand, by methane rich liquid phase transfer lime 96a and by after reducing valve 96d decompression, sending into interchanger 300 condensations, delivered to LNG storage tank 1800 by LNG transfer lime 96b after interchanger 300 condenses to the temperature that meets LNG accumulating requirement.
The rich CO cut of the liquid state 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 CO rich solution tank 900 and carry out flash distillation by the rich CO cut of liquid state transfer lime 70, the liquid and gas that after flash distillation, formation temperature is-180～-195 ℃, liquid phase is gone out by CO rich solution tank 900 tank underflows, deliver to condenser 600 cold junctions of methane rectifying tower 500 tower tops by liquid phase transfer lime 72, for it, after being provided, cold returns, after the gas phase of bringing by gas-phase transport pipe 73 is mixed, send into after cold is reclaimed in the interior re-heat of interchanger 300 and send by exhaust pipe 76 by gas-phase transport arm 75, with send into the interior further re-heat of interchanger 200 after the gas phase by after the 90 methane rectifying tower return tank 1500 gas-liquid flash distillations of gas-phase transport pipe is mixed and reclaim cold, sending in interchanger 100 a step re-heat again by exhaust pipe 77 again reclaims after 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 tower top outflow rectifying of methane rectifying tower 500 by gas-phase transport pipe 80, after with entering condenser 600, the interior liquid phase of-180～-195 ℃ is carried 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 meet the requirement of self, so need to come into operation, the Claude circularly cooling is produced the LNG product for system provides cold, whole circulation loop adopts circulating water to take away heat, and without out-of-bounds inputting the low temperature cold.But, consider the fluctuation of production process, the drawback that may exist in operation, the method is supplemented pipe 941 to the interior supplementary liquid nitrogen of CO rich solution tank 900, the cold deficiency that may cause to eliminate above-mentioned reason by liquid nitrogen.
Embodiment 6
Referring to Fig. 9, Fig. 9 has provided liquid nitrogen washing and has purified the another kind of device schema of preparing ammonia synthetic fresh gas coproduction SNG and LNG.
The difference of this embodiment and embodiment 3 is exactly: the other end of high pressure nitrogen transfer lime 12 separates two strands, one high pressure nitrogen transfer lime 12a is connected with the condensation entrance 320 of interchanger 300, and another gang of high pressure nitrogen transfer lime 12b directly is connected with virgin gas transfer lime 51.321 of the condensation outlets of interchanger 300 separate high pressure low temperature liquid nitrogen transfer lime 20, do not separate 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 conveying adapter 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 the load of interchanger 200,300 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 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 thermal source of the high pressure nitrogen of the second heat exchanger exit as the methane rectifying tower, and the cold of methane rectifying tower tower top condenser still comes from the liquid phase of CO rich solution tank.
The process distinction of this embodiment and embodiment is: through the further cooled high pressure nitrogen of interchanger 200, be divided into two strands, one is sent into by high pressure nitrogen transfer lime 12a, and in interchanger 300, a step is cooling again, and final formation temperature is-180～-190 ℃ of high pressure low temperature liquid nitrogens.Remove CO, Ar, CH 4gas phase after impurity is flowed out by nitrogen wash column 400 tower tops, by gas-phase transport pipe 50, sends into interchanger 300 re-heats, after re-heat, removes CO, Ar, CH 4form virgin gas after another strand of high pressure nitrogen that gas phase after impurity is brought with high pressure nitrogen transfer lime 12b mixes, the hydrogen nitrogen ratio of virgin gas is 2.9～3.1.Liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank 800, after constant enthalpy reducing valve 42 constant enthalpys are decompressed to 0.25～0.35MPa, do not need to turn back in interchanger 300 and carry out re-heat by liquid phase transfer lime 41, but directly by liquid phase, carry adapter 43 to enter in methane rectifying tower 500 and made with extra care by methane rectifying tower 500 tower tops.
Referring to Figure 10, in above-described embodiment, methane rectifying tower tower top condenser 600 can be built in methane rectifying tower 500, the hot junction outlet of the gaseous phase outlet at methane rectifying tower 500 tops and methane rectifying tower tower top condenser 600 shares.

Claims (29)

1. liquid nitrogen washing purifies the method for preparation ammonia synthetic fresh gas coproduction SNG, it is characterized in that, send in the raw material flash tank after the second interchanger and the 3rd interchanger are cooled to-180～-190 ℃ from the raw hydrogen of molecular sieve and carry out flash distillation and obtain the first gas phase and the first liquid phase; The first gas phase after flash distillation enters into the nitrogen wash column bottom by the tank deck outflow of raw material flash tank; High pressure nitrogen be divided into two strands after First Heat Exchanger, the second interchanger are cooling in the middle of high pressure nitrogens, it is-180～-190 ℃ of high pressure low temperature liquid nitrogens that one middle high pressure nitrogen is sent into the cooling rear formation temperature of the 3rd interchanger, this high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column, removes CO, Ar, CH in described the first gas phase 4impurity, form and remove CO, Ar, CH 4the second gas phase after impurity and liquid rich CO cut;
Remove CO, Ar, CH 4the second gas phase after impurity is flowed out by the nitrogen wash column tower top; The second gas phase flowed out by the nitrogen wash column tower top with high pressure nitrogen in the middle of another strand, mixes regulate hydrogen nitrogen compare to 2.9～3.1 and after the second interchanger re-heat formation temperature be-50～-65 ℃ of first virgin gases;
The first virgin gas is divided into two strands, one first virgin gas obtains the second virgin gas that temperature is-55～-70 ℃ after delivering to the reboiler cooling at the bottom of the methane rectifying tower, and it is 25～35 ℃ of the 3rd virgin gas that described the second virgin gas is delivered to low-temperature rectisol workshop section re-heat to temperature; Another burst first virgin gas again after the First Heat Exchanger re-heat formation temperature be 25～35 ℃ of the 4th virgin gas, the 4th virgin gas is mixed formation ammonia synthetic fresh gas afterwards and is delivered to synthetic ammonia workshop section with the 3rd virgin gas;
The first liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank, after constant enthalpy is decompressed to 0.25～0.35MPa, by the top of described methane rectifying tower, is delivered in the methane rectifying tower and is carried out methane rectifying; Methane rich liquid phase after methane rectifying is gone out by the tower bottom flow of described methane rectifying tower, after the second interchanger, First Heat Exchanger re-heat to 35 ℃, delivers to the SNG storage tank; The 3rd gas phase after methane rectifying is flowed out by the tower top of described methane rectifying tower;
The rich CO cut of described liquid state is gone out by the tower bottom flow of nitrogen wash column, tower bottom flow by nitrogen wash column goes out liquid rich CO cut after constant enthalpy is decompressed to 0.25～0.35MPa, deliver in CO rich solution tank and carry out flash distillation, the 3rd liquid phase that after flash distillation, formation temperature is-180～-195 ℃ and the 4th gas phase, the 3rd liquid phase is gone out to deliver to the condenser cold junction of described methane rectifying tower tower top by CO rich solution tank tank underflow, carry out heat exchange with the 3rd gas phase that tower top by described methane rectifying tower flows out in described condenser, the 3rd liquid phase forms the 5th gas phase after self heating up in described condenser and gasifying, the 5th gas phase is mixed and is formed the 6th gas phase of-150～-160 ℃ by the 3rd interchanger re-heat with the 4th gas phase flowed out by CO rich solution tank tank deck, the 3rd gas phase flowed out by the tower top of described methane rectifying tower forms the 4th liquid phase and delivers to the return tank of methane rectifying tower tower top and carry out the gas-liquid flash distillation in described condenser after condensation, the 7th gas phase after the gas-liquid flash distillation is mixed with described the 6th gas phase by the second interchanger, First Heat Exchanger re-heat to 25～35 ℃ formation tail gas and sent to gas ductwork, the 5th liquid phase after the gas-liquid flash distillation is as the methane rectifying column top return.
2. liquid nitrogen washing purification preparation ammonia as claimed in claim 1 synthesizes the method for virgin gas coproduction SNG only, it is characterized in that, the methane rich liquid phase gone out by the tower bottom flow of described methane rectifying tower is divided into two strands, and one methane-rich liquid continues to deliver to the SNG storage tank mutually after the second interchanger, First Heat Exchanger re-heat to 25～35 ℃; Another strand of methane-rich liquid forms the high-pressure gas that required pressure, temperature are 25～35 ℃ and sends to battery limit (BL) by the supercharging of liquid methane pump and after the second interchanger, First Heat Exchanger re-heat.
3. liquid nitrogen washing purification preparation ammonia as claimed in claim 1 synthesizes the method for virgin gas coproduction SNG only, it is characterized in that the 5th liquid-phase reflux methane rectifying tower tower top total reflux after described gas-liquid flash distillation.
4. liquid nitrogen washing purification preparation ammonia as claimed in claim 1 synthesizes the method for virgin gas coproduction SNG only, it is characterized in that, in described CO rich solution tank, supplements liquid nitrogen.
5. liquid nitrogen washing purification preparation ammonia as claimed in claim 1 synthesizes the method for virgin gas coproduction SNG only, it is characterized in that, the first liquid phase after described flash distillation is gone out by the tank underflow of raw material flash tank, carry out re-heat by the 3rd interchanger after constant enthalpy is decompressed to 0.25～0.35MPa, re-heat to the second liquid phase of-150～-160 ℃ is delivered in the methane rectifying tower and is carried out methane rectifying by the top of described methane rectifying tower; Described high pressure nitrogen formation temperature after First Heat Exchanger, the second interchanger and the 3rd interchanger are cooling is-180～-190 ℃ of high pressure low temperature liquid nitrogens, this high pressure low temperature liquid nitrogen is divided into two strands, and one high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column; Another strand of high pressure low temperature liquid nitrogen return in the 3rd interchanger with the second gas phase flowed out by the nitrogen wash column tower top in the 3rd interchanger, mixes regulate hydrogen nitrogen compare to 2.9～3.1 and after the 3rd interchanger, the second interchanger re-heat formation temperature be-50～-65 ℃ of first virgin gases.
6. liquid nitrogen washing purifies the method for preparation ammonia synthetic fresh gas coproduction LNG, it is characterized in that, send in the raw material flash tank after the second interchanger and the 3rd interchanger are cooled to-180～-190 ℃ from the raw hydrogen of molecular sieve and carry out flash distillation and obtain the first gas phase and the first liquid phase; The first gas phase after flash distillation enters into the nitrogen wash column bottom by the tank deck outflow of raw material flash tank; High pressure nitrogen in the middle of high pressure nitrogen forms after First Heat Exchanger, the second interchanger are cooling, this centre high pressure nitrogen is divided into two strands, it is-180～-190 ℃ of high pressure low temperature liquid nitrogens that one middle high pressure nitrogen is sent into the cooling rear formation temperature of the 3rd interchanger, this high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column, removes CO, Ar, CH in described the first gas phase 4impurity, form and remove CO, Ar, CH 4the second gas phase after impurity and liquid rich CO cut;
Remove CO, Ar, CH 4the second gas phase after impurity is flowed out by the nitrogen wash column tower top; The second gas phase flowed out by the nitrogen wash column tower top is mixed and is regulated hydrogen nitrogen ratio to 2.9～3.1 with high pressure nitrogen in the middle of another strand, and formation temperature is-45～-65 ℃ of first virgin gases after the second interchanger re-heat;
The first virgin gas is divided into two strands, one first virgin gas obtains the second virgin gas that temperature is-50～-70 ℃ after delivering to the reboiler cooling at the bottom of the methane rectifying tower, and it is 25～35 ℃ of the 3rd virgin gas that described the second virgin gas is delivered to low-temperature rectisol workshop section re-heat to temperature; Another burst first virgin gas again after the First Heat Exchanger re-heat formation temperature be 25～35 ℃ of the 4th virgin gas, the 4th virgin gas is mixed formation ammonia synthetic fresh gas afterwards and is delivered to synthetic ammonia workshop section with the 3rd virgin gas;
The first liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank, after constant enthalpy is decompressed to 0.25～0.35MPa, by the top of described methane rectifying tower, is delivered in the methane rectifying tower and is carried out methane rectifying; Methane rich liquid phase after methane rectifying is gone out by the tower bottom flow of described methane rectifying tower, after the supercharging of liquid methane pump, is divided into two strands, one methane rich liquid phase;
The high-pressure gas that the required pressure of formation, temperature are 25～35 ℃ after the second interchanger, First Heat Exchanger re-heat is sent to battery limit (BL); Another strand of methane-rich liquid crossed and is as cold as-162 ℃ and delivers to the LNG storage tank by the 3rd interchanger; The 3rd gas phase after methane rectifying is flowed out by the tower top of described methane rectifying tower;
The rich CO cut of described liquid state is gone out by the tower bottom flow of nitrogen wash column, tower bottom flow by nitrogen wash column goes out liquid rich CO cut after constant enthalpy is decompressed to 0.25～0.35MPa, deliver in CO rich solution tank and carry out flash distillation, the 3rd liquid phase that after flash distillation, formation temperature is-180～-195 ℃ and the 4th gas phase, the 3rd liquid phase is gone out to deliver to the condenser cold junction of described methane rectifying tower tower top by CO rich solution tank tank underflow, carry out heat exchange with the 3rd gas phase that tower top by described methane rectifying tower flows out in described condenser, the 3rd liquid phase forms the 5th gas phase after self heating up in described condenser and gasifying, the 5th gas phase is mixed and is formed the 6th gas phase of-150～-160 ℃ by the 3rd interchanger re-heat with the 4th gas phase flowed out by CO rich solution tank tank deck, the 3rd gas phase flowed out by the tower top of described methane rectifying tower forms the 4th liquid phase and delivers to the return tank of methane rectifying tower tower top and carry out the gas-liquid flash distillation in described condenser after condensation, the 7th gas phase after the gas-liquid flash distillation is mixed with described the 6th gas phase by the second interchanger, First Heat Exchanger re-heat to 25～35 ℃ formation tail gas and sent to gas ductwork, the 5th liquid phase after the gas-liquid flash distillation is as the methane rectifying column top return.
7. liquid nitrogen washing as claimed in claim 6 purifies the method for preparation ammonia synthetic fresh gas coproduction LNG, it is characterized in that, set up a Claude cycle refrigeration system between described First Heat Exchanger and the second interchanger, for system provides cold, produce the LNG product.
8. liquid nitrogen washing as claimed in claim 6 purifies the method for preparation ammonia synthetic fresh gas coproduction LNG, it is characterized in that the 5th liquid-phase reflux methane rectifying tower tower top total reflux after described gas-liquid flash distillation.
9. liquid nitrogen washing as claimed in claim 6 purifies the method for preparation ammonia synthetic fresh gas coproduction LNG, it is characterized in that, the first liquid phase after described flash distillation is gone out by the tank underflow of raw material flash tank, carry out re-heat by the 3rd interchanger after constant enthalpy is decompressed to 0.25～0.35MPa, re-heat to the second liquid phase of-150～-160 ℃ is delivered in the methane rectifying tower and is carried out methane rectifying by the top of described methane rectifying tower; Described high pressure nitrogen formation temperature after First Heat Exchanger, the second interchanger and the 3rd interchanger are cooling is-180～-190 ℃ of high pressure low temperature liquid nitrogens, this high pressure low temperature liquid nitrogen is divided into two strands, and one high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column; Another strand of high pressure low temperature liquid nitrogen return in the 3rd interchanger with the second gas phase flowed out by the nitrogen wash column tower top in the 3rd interchanger, mixes regulate hydrogen nitrogen compare to 2.9～3.1 and after the 3rd interchanger, the second interchanger re-heat formation temperature be-50～-65 ℃ of first virgin gases.
10. liquid nitrogen washing purifies the method for preparation ammonia synthetic fresh gas coproduction SNG and LNG, it is characterized in that, send in the raw material flash tank after the second interchanger and the 3rd interchanger are cooled to-180～-190 ℃ from the raw hydrogen of molecular sieve and carry out flash distillation and obtain the first gas phase and the first liquid phase; The first gas phase after flash distillation enters into the nitrogen wash column bottom by the tank deck outflow of raw material flash tank; High pressure nitrogen in the middle of high pressure nitrogen forms after First Heat Exchanger, the second interchanger are cooling, this centre high pressure nitrogen is divided into two strands, it is-180～-190 ℃ of high pressure low temperature liquid nitrogens that one middle high pressure nitrogen is sent into the cooling rear formation temperature of the 3rd interchanger, this high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column, removes CO, Ar, CH in described the first gas phase 4impurity, form and remove CO, Ar, CH 4the second gas phase after impurity and liquid rich CO cut;
Remove CO, Ar, CH 4the second gas phase after impurity is flowed out by the nitrogen wash column tower top; The second gas phase flowed out by the nitrogen wash column tower top is mixed and is regulated hydrogen nitrogen ratio to 2.9～3.1 with high pressure nitrogen in the middle of another strand, and formation temperature is-45～-65 ℃ of first virgin gases after the second interchanger re-heat;
The first virgin gas is divided into two strands, one first virgin gas obtains the second virgin gas that temperature is-50～-70 ℃ after delivering to the reboiler cooling at the bottom of the methane rectifying tower, and it is 25～35 ℃ of the 3rd virgin gas that described the second virgin gas is delivered to low-temperature rectisol workshop section re-heat to temperature; Another burst first virgin gas again after the First Heat Exchanger re-heat formation temperature be 25～35 ℃ of the 4th virgin gas, the 4th virgin gas is mixed formation ammonia synthetic fresh gas afterwards and is delivered to synthetic ammonia workshop section with the 3rd virgin gas;
The first liquid phase after flash distillation is gone out by the tank underflow of raw material flash tank, after constant enthalpy is decompressed to 0.25～0.35MPa, by the top of described methane rectifying tower, is delivered in the methane rectifying tower and is carried out methane rectifying; Methane rich liquid phase after methane rectifying is gone out by the tower bottom flow of described methane rectifying tower, go out the methane rich liquid phase by the tower bottom flow of described methane rectifying tower and be divided into two strands, wherein one methane rich liquid phase is delivered to the SNG storage tank after the second interchanger, First Heat Exchanger re-heat to 35 ℃; Another strand of methane-rich liquid is divided into two thighs after the supercharging of liquid methane pump, and thigh methane rich liquid phase forms the high-pressure gas that required pressure, temperature are 25～35 ℃ and sends to battery limit (BL) after the second interchanger, First Heat Exchanger re-heat; Another thigh methane-rich liquid is crossed and is as cold as-162 ℃ and delivers to the LNG storage tank by the 3rd interchanger; The 3rd gas phase after methane rectifying is flowed out by the tower top of described methane rectifying tower;
The rich CO cut of described liquid state is gone out by the tower bottom flow of nitrogen wash column, tower bottom flow by nitrogen wash column goes out liquid rich CO cut after constant enthalpy is decompressed to 0.25～0.35MPa, deliver in CO rich solution tank and carry out flash distillation, the 3rd liquid phase that after flash distillation, formation temperature is-180～-195 ℃ and the 4th gas phase, the 3rd liquid phase is gone out to deliver to the condenser cold junction of described methane rectifying tower tower top by CO rich solution tank tank underflow, carry out heat exchange with the 3rd gas phase that tower top by described methane rectifying tower flows out in described condenser, the 3rd liquid phase forms the 5th gas phase after self heating up in described condenser and gasifying, the 5th gas phase is mixed and is formed the 6th gas phase of-150～-160 ℃ by the 3rd interchanger re-heat with the 4th gas phase flowed out by CO rich solution tank tank deck, the 3rd gas phase flowed out by the tower top of described methane rectifying tower forms the 4th liquid phase and delivers to the return tank of methane rectifying tower tower top and carry out the gas-liquid flash distillation in described condenser after condensation, the 7th gas phase after the gas-liquid flash distillation is mixed with described the 6th gas phase by the second interchanger, First Heat Exchanger re-heat to 25～35 ℃ formation tail gas and sent to gas ductwork, the 5th liquid phase after the gas-liquid flash distillation is as the methane rectifying column top return.
11. liquid nitrogen washing as claimed in claim 10 purifies the method for preparation ammonia synthetic fresh gas coproduction SNG and LNG, it is characterized in that, set up a Claude cycle refrigeration system or/and supplement liquid nitrogen in described CO rich solution tank between described First Heat Exchanger and the second interchanger, for system provides cold, produce the LNG/SNG product.
12. liquid nitrogen washing as claimed in claim 10 purifies the method for preparation ammonia synthetic fresh gas coproduction SNG and LNG, it is characterized in that the 5th liquid-phase reflux methane rectifying tower tower top total reflux after described gas-liquid flash distillation.
13. liquid nitrogen washing as claimed in claim 10 purifies the method for preparation ammonia synthetic fresh gas coproduction SNG and LNG, it is characterized in that, the first liquid phase after described flash distillation is gone out by the tank underflow of raw material flash tank, carry out re-heat by the 3rd interchanger after constant enthalpy is decompressed to 0.25～0.35MPa, re-heat to the second liquid phase of-150～-160 ℃ is delivered in the methane rectifying tower and is carried out methane rectifying by the top of described methane rectifying tower; Described high pressure nitrogen formation temperature after First Heat Exchanger, the second interchanger and the 3rd interchanger are cooling is-180～-190 ℃ of high pressure low temperature liquid nitrogens, this high pressure low temperature liquid nitrogen is divided into two strands, and one high pressure low temperature liquid nitrogen is directly delivered to inner the first gas phase counter current contact with entering in nitrogen wash column of nitrogen wash column; Another strand of high pressure low temperature liquid nitrogen return in the 3rd interchanger with the second gas phase flowed out by the nitrogen wash column tower top in the 3rd interchanger, mixes regulate hydrogen nitrogen compare to 2.9～3.1 and after the 3rd interchanger, the second interchanger re-heat formation temperature be-50～-65 ℃ of first virgin gases.
14. realize that liquid nitrogen washing claimed in claim 1 purifies the device of the method for preparation ammonia synthetic fresh gas coproduction SNG for one kind, 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 tower top condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, C0 rich solution tank, liquid methane pump;
With sky, divide the first high pressure nitrogen transfer lime be connected to be connected with the first condensation entrance of described First Heat Exchanger, one end of the second high pressure nitrogen transfer lime is connected with the first condensation outlet of described First Heat Exchanger, 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, 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 be 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 outlet of described the second interchanger, 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 outlet of described the 3rd interchanger, the 5th condensation entrance is communicated with the 5th condensation outlet, 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 tower top is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of 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 and remove CO, Ar, CH at the top of nitrogen wash column 4the second gaseous phase outlet after 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 Yu tri-interchanger, the 3rd re-heat outlet the 3rd re-heat entrance of the 3rd interchanger is communicated with, the 3rd re-heat outlet of the 3rd interchanger is taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport, and the second gas-phase transport is taken over another burst of third high and pressed the nitrogen transfer lime to be connected; 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 is carried to take over by the second virgin gas and is connected low-temperature rectisol workshop section entrance, and the re-heat outlet of low-temperature rectisol workshop section is the 3rd virgin gas; 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 is carried to take over by the 4th virgin gas and connected ammonia synthesis workshop section, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Low-temperature rectisol workshop section also carries to take over by the 3rd virgin gas transfer lime and described the 4th virgin gas and is connected the rear ammonia synthetic fresh gas that forms;
The rich CO cut outlet of the liquid state of nitrogen wash column bottom is connected to the entrance of C0 rich solution tank by the rich CO cut of liquid state transfer lime, the top of C0 rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of C0 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 tower top condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower tower top 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 Yu tri-interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat outlet of the 3rd interchanger, 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 outlet of the second interchanger, 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 outlet of First Heat Exchanger, the 9th re-heat outlet is communicated with the 9th re-heat entrance, another termination gas ductwork of the 3rd exhaust pipe;
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 tower top condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower tower top 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, 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.
15. device as claimed in claim 14, is characterized in that, described methane rectifying tower tower top condenser is built in 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 tower top condenser.
16. device as claimed in claim 14, it is characterized in that, also comprise a methane rectifying tower return tank, described methane rectifying tower tower top condenser is external outside methane rectifying tower tower top, and the hot junction outlet of described methane rectifying tower tower top condenser is connected with the entrance of methane rectifying tower return tank; Be provided with the 7th gaseous phase outlet at the top of methane rectifying tower return tank, 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 with the reflux inlet of methane rectifier by return line.
17. device as claimed in claim 14, is characterized in that, is provided with liquid nitrogen in the bottom of described C0 rich solution tank and supplements mouth, this liquid nitrogen supplements mouth and supplements pipe connecting fluid nitrogenous source by liquid nitrogen.
18. device as claimed in claim 14, it is characterized in that, described third high presses the other end of nitrogen transfer lime not separate two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the 3rd condensation outlet of described the 3rd interchanger separates the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime, on the first high pressure low temperature liquid nitrogen transfer lime after series connection one reducing valve the other end be connected to the first re-heat entrance of described the 3rd interchanger, 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 carried to take over by second liquid phase and is connected with the second liquid phase entrance of methane rectifier, 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 taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport.
19. realize that liquid nitrogen washing claimed in claim 6 purifies the device of the method for preparation ammonia synthetic fresh gas coproduction LNG for one kind, 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 tower top condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, C0 rich solution tank, liquid methane pump;
With sky, divide the first high pressure nitrogen transfer lime be connected to be connected with the first condensation entrance of described First Heat Exchanger, one end of the second high pressure nitrogen transfer lime is connected with the first condensation outlet of described First Heat Exchanger, 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, 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 be 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 outlet of described the second interchanger, 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 outlet of described the 3rd interchanger, the 5th condensation entrance is communicated with the 5th condensation outlet, 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 tower top is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of 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 and remove CO, Ar, CH at the top of nitrogen wash column 4the second gaseous phase outlet after 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 Yu tri-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 the 3rd re-heat entrance of the 3rd interchanger is communicated with, the 3rd re-heat outlet of the 3rd interchanger is taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport, and the second gas-phase transport is taken over another burst of third high and pressed the nitrogen transfer lime to be connected; 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 is carried to take over by the second virgin gas and is connected low-temperature rectisol workshop section entrance, and the re-heat outlet of low-temperature rectisol workshop section is the 3rd virgin gas; 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 is carried to take over by the 4th virgin gas and connected ammonia synthesis workshop section, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Low-temperature rectisol workshop section also carries to take over by the 3rd virgin gas transfer lime and described the 4th virgin gas and is connected the rear ammonia synthetic fresh gas that forms;
The rich CO cut outlet of the liquid state of nitrogen wash column bottom is connected to the entrance of C0 rich solution tank by the rich CO cut of liquid state transfer lime, the top of C0 rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of C0 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 tower top condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower tower top 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 Yu tri-interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat outlet of the 3rd interchanger, 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 outlet of the second interchanger, 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 outlet of First Heat Exchanger, the 9th re-heat outlet is communicated with the 9th re-heat entrance, another termination gas ductwork of the 3rd exhaust pipe;
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 tower top condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower tower top 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 on 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.
20. device as claimed in claim 19, is characterized in that, described methane rectifying tower tower top condenser is built in 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 tower top condenser.
21. device as claimed in claim 19, it is characterized in that, also comprise a methane rectifying tower return tank, described methane rectifying tower tower top condenser is external outside methane rectifying tower tower top, and the hot junction outlet of described methane rectifying tower tower top condenser is connected with the entrance of methane rectifying tower return tank; Be provided with the 7th gaseous phase outlet at the top of methane rectifying tower return tank, 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 with the reflux inlet of methane rectifier by return line.
22. device as claimed in claim 19, 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, the first cold loop head is communicated with the first cold loop exit.
23. device as claimed in claim 19, it is characterized in that, described third high presses the other end of nitrogen transfer lime not separate two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the 3rd condensation outlet of described the 3rd interchanger separates the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime, on the first high pressure low temperature liquid nitrogen transfer lime after series connection one reducing valve the other end be connected to the first re-heat entrance of described the 3rd interchanger, 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 carried to take over by second liquid phase and is connected with the second liquid phase entrance of methane rectifier, 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 taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport.
24. realize that liquid nitrogen washing claimed in claim 10 purifies the device of the method for preparation ammonia synthetic fresh gas coproduction SNG and LNG for one kind, 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 tower top condenser, methane rectifying tower tower bottom reboiler, unstripped gas flash tank, C0 rich solution tank;
With sky, divide the first high pressure nitrogen transfer lime be connected to be connected with the first condensation entrance of described First Heat Exchanger, one end of the second high pressure nitrogen transfer lime is connected with the first condensation outlet of described First Heat Exchanger, 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, 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 be 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 outlet of described the second interchanger, 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 outlet of described the 3rd interchanger, the 5th condensation entrance is communicated with the 5th condensation outlet, 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 tower top is provided with the first gaseous phase outlet, be provided with the first liquid-phase outlet at the bottom of 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 and remove CO, Ar, CH at the top of nitrogen wash column 4the second gaseous phase outlet after 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 Yu tri-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 the 3rd re-heat entrance of the 3rd interchanger is communicated with, the 3rd re-heat outlet of the 3rd interchanger is taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport, and the second gas-phase transport is taken over another burst of third high and pressed the nitrogen transfer lime to be connected; 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 is carried to take over by the second virgin gas and is connected low-temperature rectisol workshop section entrance, and the re-heat outlet of low-temperature rectisol workshop section is the 3rd virgin gas; 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 is carried to take over by the 4th virgin gas and connected ammonia synthesis workshop section, and the 6th re-heat entrance is communicated with the 6th re-heat outlet; Low-temperature rectisol workshop section also carries to take over by the 3rd virgin gas transfer lime and described the 4th virgin gas and is connected the rear ammonia synthetic fresh gas that forms;
The rich CO cut outlet of the liquid state of nitrogen wash column bottom is connected to the entrance of C0 rich solution tank by the rich CO cut of liquid state transfer lime, the top of C0 rich solution tank is provided with the 4th gaseous phase outlet, and the bottom of C0 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 tower top condenser by the 3rd liquid phase transfer lime, the cold side outlet of methane rectifying tower tower top 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 Yu tri-interchanger be connected, one end of the first exhaust pipe is connected with the 7th re-heat outlet of the 3rd interchanger, 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 outlet of the second interchanger, 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 outlet of First Heat Exchanger, the 9th re-heat outlet is communicated with the 9th re-heat entrance, another termination gas ductwork of the 3rd exhaust pipe;
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 tower top condenser by the 3rd gas-phase transport pipe, and the hot junction outlet of methane rectifying tower tower top condenser is connected with the 4th liquid phase transfer lime;
The methane rich liquid phase of methane rectifier bottoms exports and 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 on 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, 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 on 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.
25. device as claimed in claim 24, is characterized in that, described methane rectifying tower tower top condenser is built in 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 tower top condenser.
26. device as claimed in claim 24, it is characterized in that, also comprise a methane rectifying tower return tank, described methane rectifying tower tower top condenser is external outside methane rectifying tower tower top, and the hot junction outlet of described methane rectifying tower tower top condenser is connected with the entrance of methane rectifying tower return tank; Be provided with the 7th gaseous phase outlet at the top of methane rectifying tower return tank, 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 with the reflux inlet of methane rectifier by return line.
27. device as claimed in claim 24, 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 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, the first cold loop head is communicated with the first cold loop exit.
28. device as claimed in claim 24, is characterized in that, is provided with liquid nitrogen in the bottom of described C0 rich solution tank and supplements mouth, this liquid nitrogen supplements mouth and supplements pipe connecting fluid nitrogenous source by liquid nitrogen.
29. device as claimed in claim 24, it is characterized in that, described third high presses the other end of nitrogen transfer lime not separate two strands and directly directly be connected with the 3rd condensation entrance of described the 3rd interchanger, the 3rd condensation outlet of described the 3rd interchanger separates the first high pressure low temperature liquid nitrogen transfer lime and the second high pressure low temperature liquid nitrogen transfer lime, on the first high pressure low temperature liquid nitrogen transfer lime after series connection one reducing valve the other end be connected to the first re-heat entrance of described the 3rd interchanger, 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 carried to take over by second liquid phase and is connected with the second liquid phase entrance of methane rectifier, 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 taken over and is connected with the 4th re-heat entrance of the second interchanger by the second gas-phase transport.
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CN103438662A (en) * 2013-08-21 2013-12-11 河南心连心深冷能源股份有限公司 Device and technological method for LNG production through recycling synthesis ammonia tail gas
CN106352656A (en) * 2016-08-23 2017-01-25 杭州福斯达深冷装备股份有限公司 Device for preparing ammonia synthesis gas and joint production LNG using liquid nitrogen wash and method thereof
CN110482568A (en) * 2019-08-12 2019-11-22 上海国际化建工程咨询有限公司 A kind of by-product alkanol for medium and small nitrogen fertilizer factory to be transformed and the method and system of cold and hot joint purification
CN111676069A (en) * 2020-06-18 2020-09-18 中冶西北工程技术有限公司 Coke oven gas purification system

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103438662A (en) * 2013-08-21 2013-12-11 河南心连心深冷能源股份有限公司 Device and technological method for LNG production through recycling synthesis ammonia tail gas
CN106352656A (en) * 2016-08-23 2017-01-25 杭州福斯达深冷装备股份有限公司 Device for preparing ammonia synthesis gas and joint production LNG using liquid nitrogen wash and method thereof
CN106352656B (en) * 2016-08-23 2018-10-09 杭州福斯达深冷装备股份有限公司 It is a kind of with the devices and methods therefor of liquid nitrogen washing ammonia synthesis gas coproduction LNG
CN110482568A (en) * 2019-08-12 2019-11-22 上海国际化建工程咨询有限公司 A kind of by-product alkanol for medium and small nitrogen fertilizer factory to be transformed and the method and system of cold and hot joint purification
CN111676069A (en) * 2020-06-18 2020-09-18 中冶西北工程技术有限公司 Coke oven gas purification system
CN111676069B (en) * 2020-06-18 2021-05-04 中冶西北工程技术有限公司 Coke oven gas purification system

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