CN102654348B - Method for producing liquefied natural gas by using coke oven gas - Google Patents
Method for producing liquefied natural gas by using coke oven gas Download PDFInfo
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- CN102654348B CN102654348B CN201210159925.1A CN201210159925A CN102654348B CN 102654348 B CN102654348 B CN 102654348B CN 201210159925 A CN201210159925 A CN 201210159925A CN 102654348 B CN102654348 B CN 102654348B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—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
- F25J3/0257—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 nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/14—Coke-ovens gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a method for producing liquefied natural gas by using coke oven gas, comprising the following steps of: (1) compressing and cooling coke oven gas raw material gas; (2) dividing the cooled coke oven gas into two paths, i.e., a coke oven gas material flow A and a coke oven gas material flow B, cooling the coke oven gas material flow B, mixing the cooled coke oven gas material flow B with the coke oven gas material flow A, and then conveying the two coke oven gas material flows in a heat exchanger group to perform heat exchange; (3) conveying coke oven gas exhausted from the heat exchanger group in a gas-liquid separation tank; and (4) conveying material flows drained from the bottom of the gas-liquid separation tank in a rectifying tower, conveying material flows of the bottom of the rectifying tower in a reboiler arranged on the bottom of the rectifying tower, throttling material flows from the reboiler via a J-T valve, so as to obtain a product. The invention discloses a method adopting low-temperature rectifying by combining the current situation of the utilization of coke oven gas in China, used for separating methane from coke oven gas and producing the methane into the liquefied natural gas; and the whole process has the advantages of being simple in flow, convenient for operation, high in recovery rate of the methane, high in purity of a LNG (liquefied natural gas) product, and low in overall energy consumption.
Description
Technical field
The present invention relates to a kind of method of preparing liquefied natural gas from coke oven gas.
Background technology
Annual China is accumulative produces 3 ~ 400,000,000 tons, coke, and by ton, Jiao produces 420m
3coke-stove gas calculates, and coke-stove gas output is 1,449 hundred million m
3.Because the coke-oven plant of most of iron and steel enterprise of China uses BF gas heating coke oven, substantially coke-stove gas is fully utilized, and independently about there is the coke-stove gas of half coke-oven plant for coke oven conducting self-heating, the coke-stove gas of half is outwards carried or is arranged special device and reclaims in addition.Estimate that the coal chemical enterprise in the whole nation is at least outwards carried every year or needs the amount arranging special arrangement recovery coke-stove gas to be 30,000,000,000 m
3, tradition utilizes oven gas methanol, and owing to affecting by factors such as markets, supply exceed demand for current methanol market, utilizes the device benefit of coke-stove gas methanol not high.So a large amount of coke-stove gas, how rationally, efficiently, clean utilization, be a very urgent vital task.
Containing a large amount of H in coke-stove gas
2, CH
4, the fuel gas such as CO, if reasonably utilized by these gases, both can alleviate the present situation of domestic energy deficiency, good economic benefit can be brought for coal chemical enterprise again.
Produce liquefied natural gas (LNG) if can be used to after oven gas deep purifying, methanation and dehydration, if annual China reclaims the oven gas that 300 billion cubic meters diffuse, about 130 billion cubic meter natural gases can be obtained, and reduce discharging a large amount of methane, SO
2and the harmful substance such as tar, naphthalene, ammonia.Therefore, coke-stove gas LNG project not only effectively can alleviate the problem of domestic natural gas shortage, and will technological progress and the industry development of coking and energy industry be promoted, development oven gas LNG project produces obvious economic benefit, environmental benefit and social benefit, recycles industry significant for oven gas.
The typical case of coke-stove gas forms as shown in table 1, and the composition of itself and conventional gas has very large difference, and Qi Zhongqing, nitrogen content are relatively high, and relatively and conventional gas, production LNG product energy consumption is higher, and liquefaction process is also more complicated.
Typical case's composition of table 1 coke-stove gas
| Composition V% | H 2 | CH 4 | CO | N 2 | CO 2 | C nH m | O 2 | Calorific value Mj/Nm 3 |
| Content | 54~59 | 24~28 | 5.5~7 | 3~5 | 1~3 | 2~3 | 0.3~0.7 | ~17 |
Summary of the invention
The object of this invention is to provide a kind of method of preparing liquefied natural gas from coke oven gas, the liquefied natural gas purity that this method is produced can reach more than 99%, and whole set process is simple, easy to operate, can solve the recovery problem of coke-stove gas well.
The method of a kind of preparing liquefied natural gas from coke oven gas provided by the present invention, comprises the steps:
(1) coke-stove gas is carried out compressing and cooling;
(2) two strands will be divided into through cooled coke-stove gas: coke-stove gas material flow A and coke-stove gas flow B; Described coke-stove gas flow B enters heat exchanger package after mixing with described coke-stove gas material flow A after cooling and carries out exchange heat;
(3) out knockout drum is entered to afterwards from described heat exchanger package coke-stove gas out;
(4) logistics out of the bottom of described knockout drum enters rectifying column; The tower base stream of described rectifying column enters to the reboiler be arranged at the bottom of described rectifying tower; From described reboiler, namely logistics out obtains liquefied natural gas through the throttling of J-T valve again.
In above-mentioned method, the logistics of described gas-liquid separation pot bottom enters to described rectifying column from the middle part of described rectifying column.
In above-mentioned method, from described reboiler, logistics out obtains liquefied natural gas through the throttling of described J-T valve again after cooling.
In above-mentioned method, logistics out from described reboiler is cooled to-150 DEG C ~-162 DEG C, as-160 DEG C.
In above-mentioned method, the cold of described heat exchanger package is provided by refrigeration system; Described refrigeration system can be gas expansion refrigeration system or azeotrope refrigeration system.
In above-mentioned method, in step (2), described coke-stove gas flow B is cooled to-20 DEG C ~-120 DEG C, as-120 DEG C, described cooling procedure provides heat for described reboiler.
In above-mentioned method, after described coke-stove gas material flow A and the mixing of coke-stove gas flow B, be cooled to-140 DEG C ~-160 DEG C, as-155 DEG C through described heat exchanger package.
In above-mentioned method, from the top of described knockout drum, logistics is out through described heat exchanger package rewarming.
In above-mentioned method, eject next logistics through described heat exchanger package rewarming from described rectifying tower.
The present invention proposes in conjunction with the present situation that China's coke-stove gas utilizes the method adopting cryogenic rectification, methane is separated from coke-stove gas, make liquefied natural gas, whole set process have that flow process is simple, easy to operate, the advantage that purity is high, overall energy consumption is low of methane recovery and LNG product.
Accompanying drawing explanation
Fig. 1 and Fig. 2 is azeotrope kind of refrigeration cycle in the embodiment of the present invention 1 and produces the schematic flow sheet of LNG;
Fig. 3 is the schematic flow sheet that in the embodiment of the present invention 2, gas expansion kind of refrigeration cycle produces LNG.
Detailed description of the invention
The experimental technique used in following embodiment if no special instructions, is conventional method.
Material used in following embodiment, reagent etc., if no special instructions, all can obtain from commercial channels.
Embodiment 1,
The present embodiment is adopt a kind of schematic flow sheet that mixed working fluid freezes, rectification method produces LNG.
As shown in Figure 1, this technological process mainly comprises refrigeration system, heat transmission equipment and separation equipment; Wherein refrigeration plant is gas compressor and J-T valve, and heat transmission equipment comprises ice chest and air cooling/water cooling heat exchanger, and separation equipment comprises knockout drum and rectifying column; Rectifying column is provided with reboiler and condenser, improves the purity of LNG further and increases methane recovery; This cover technique also comprises azeotrope compressor and condenser.
Its technological process is as follows:
As shown in Figure 1: will containing H
2, N
2coke-stove gas through cooler E-100 cool after be divided into two bursts of material flow A and B, coke-stove gas flow B is cooled to about-120 DEG C through reboiler E-102, after rectifying column T-100 bottom reboiler provides thermal source, mix with coke-oven coal material flow A, after heat exchanger E-101 is cooled to-155 DEG C, enter knockout drum V-100, isolate most of H through knockout drum V-100
2after liquid phase stream 1, rectifying column T-100 is entered from middle part, in logistics in rectifying column T-100 after sufficient matter, heat exchange, rectifying column T-100 Base top contact is based on the periodic off-gases of nitrogen and hydrogen, and rectifying column T-100 tower bottom logistics 15 obtains highly purified liquified natural gas through the throttling of J-T valve; Successively enter heat exchanger E-101 and E-100 from the isolated gas stream 2 of knockout drum V-100, for this two heat exchanger provides part low-temperature receiver, the temperature rewarming of logistics 3 is to normal temperature.The gas stream 4 of rectifying column T-100 Base top contact enters the condenser E-103 of rectifying column, and the methane in logistics 4, after E-103 condensation, enters gas-liquid separator V-102, and liquid stream 5 returns rectifying column, as the phegma of rectifying column; The gas stream 6 be separated in V-102, based on nitrogen and hydrogen, enters E-101 and E-100 successively, and temperature rewarming is to normal temperature.Azeotrope working medium logistics 7 is after compressor C-100 compresses and cooler E-104 cools, enter gas-liquid separator V-101 and isolate liquid stream 8 and gaseous stream 9, gaseous stream compresses through compressor C-101, liquid stream pressurizes through liquor pump P-100, enter in cooler E-105 after two strands of liquid joint and be cooled to normal temperature, the two-phase mixtures refrigeration working medium logistics 10 of normal temperature and high pressure enters heat exchanger E-100 and E-101 successively, from E-101, the temperature of logistics 11 out reaches-155 DEG C, be divided into two bursts of logistics 12 and logistics 13, condenser E-103 for rectifying column after logistics 12 throttling refrigeration provides low-temperature receiver, from E-103, after logistics out 14 and logistics 13 throttling, logistics converges, enter E-101 and E-100 successively, for oven gas cooling and condensation provide low-temperature receiver.
As shown in Figure 2: will containing H
2, N
2coke-stove gas through cooler E-100 cool after be divided into two bursts of material flow A and B, coke-stove gas flow B is cooled to about-120 DEG C through reboiler E-102, after rectifying column T-100 bottom reboiler provides thermal source, mix with coke-oven coal material flow A, after heat exchanger E-101 is cooled to-150 DEG C, enter knockout drum V-100, isolate most of H through knockout drum V-100
2after liquid phase stream 1, rectifying column T-100 is entered from middle part, in logistics in rectifying column T-100 after sufficient matter, heat exchange, rectifying column T-100 Base top contact is based on the periodic off-gases of nitrogen and hydrogen, and rectifying column T-100 tower bottom logistics 16 enters in heat exchanger E-106 and cools, and is cooled to about-160 DEG C, highly purified liquified natural gas is obtained again through the throttling of J-T valve, increase liquefied natural gas cross cold after, reduce the flashed vapour scale of construction after throttling, flash gas treatment system reduces; Enter from the isolated gas stream 2 of knockout drum V-100 and successively enter heat exchanger E-101 and E-100, for this two heat exchanger provides part low-temperature receiver, the temperature rewarming of logistics 3 is to normal temperature.The gas stream 4 that rectifying column T-100 top causes enters the condenser E-103 of rectifying column, and the methane in logistics 4, after E-103 condensation, enters gas-liquid separator V-102, and liquid stream 5 returns rectifying column, as the phegma of rectifying column; The gas stream 6 be separated in V-102, based on nitrogen and hydrogen, enters E-101 and E-100 successively, and temperature rewarming is to normal temperature.Azeotrope working medium logistics 7 is after compressor C-100 compresses and cooler E-104 cools, enter gas-liquid separator V-101 and isolate liquid stream 8 and gaseous stream 9, gaseous stream compresses through compressor C-101, liquid stream pressurizes through liquor pump P-100, enter in cooler E-105 after two strands of liquid joint and be cooled to normal temperature, the two-phase mixtures refrigeration working medium logistics 10 of normal temperature and high pressure enters heat exchanger E-100 and E-101 successively, from E-101, the temperature of logistics 11 out reaches-160 DEG C, be divided into two bursts of logistics 12 and logistics 13, condenser E-103 for rectifying column after logistics 12 throttling refrigeration provides low-temperature receiver, for heat exchanger E-106 provides cold after logistics 13 throttling refrigeration, from E-103 and E-106, logistics out 14 and logistics 15 converge, enter E-101 and E-100 successively, for oven gas cooling and condensation provide low-temperature receiver.
Embodiment 2,
A kind of schematic flow sheet that the present embodiment is employing nitrogen swell refrigeration, rectification method produces LNG.
As shown in Figure 3, this technological process mainly comprises refrigeration system, heat transmission equipment and separation equipment; Wherein refrigeration plant is gas compressor and decompressor, and heat transmission equipment comprises ice chest and air cooling/water cooling heat exchanger, and separation equipment comprises knockout drum tank and rectifying column; Rectifying column is provided with reboiler and condenser, improves the purity of LNG and the rate of recovery of methane further.This cover technique also comprises N
2compressor and condenser, nitrogen expansion refrigeration system provides low-temperature receiver for whole set process.
Idiographic flow is: will containing H
2, N
2coke-stove gas through cooler E-100 cool after be divided into two bursts of material flow A and B, coke-stove gas flow B is cooled to about-120 DEG C through reboiler E-102, after rectifying column T-100 bottom reboiler provides thermal source, mix with coke-oven coal material flow A, after heat exchanger E-101 is cooled to-155 DEG C, enter knockout drum V-100, isolate most of H through knockout drum V-100
2after liquid phase stream 1, rectifying column T-100 is entered from middle part, in logistics in rectifying column T-100 after sufficient matter, heat exchange, rectifying column T-100 Base top contact is based on the periodic off-gases of nitrogen and hydrogen, and rectifying column T-100 tower bottom logistics 13 obtains highly purified liquified natural gas through the throttling of J-T valve; Enter from the isolated gas stream 2 of knockout drum V-100 and successively enter heat exchanger E-101 and E-100, for this two heat exchanger provides part low-temperature receiver, the temperature rewarming of logistics 3 is to normal temperature.The gas stream 4 of rectifying column T-100 Base top contact enters the condenser E-103 of rectifying column, and the methane in logistics 4, after E-103 condensation, enters gas-liquid separator V-102, and liquid stream 5 returns rectifying column, as the phegma of rectifying column; The gas stream 6 be separated in V-101, based on nitrogen and hydrogen, enters E-101 and E-100 successively, and temperature rewarming is to normal temperature.Nitrogen stream 7 is after compressor C-100 compresses and cooler E-104 cools, enter after continuing compression in the supercharger C-101 of turbo-expander EXP-100, enter the logistics 9 after being cooled to normal temperature in cooler E-105 and enter heat exchanger E-100 and E-101 successively, from E-101, the temperature of logistics 10 out reaches about-120 DEG C, enter swell refrigeration in turbo-expander EXP-100, the temperature of logistics 11 reaches about-170 DEG C, for the condenser E-103 of rectifying column provides low-temperature receiver, from E-103, logistics 12 out enters E-101 and E-100 more successively, for oven gas cooling and condensation provide low-temperature receiver.
Claims (2)
1. a method for preparing liquefied natural gas from coke oven gas, comprises the steps:
(1) coke-stove gas unstripped gas is carried out compression cooling;
(2) two strands will be divided into through cooled coke-stove gas: coke-stove gas material flow A and coke-stove gas flow B; Described coke-stove gas flow B enters heat exchanger package after mixing with described coke-stove gas material flow A after cooling and carries out exchange heat;
The cold of described heat exchanger package is provided by a set of refrigeration system; Described refrigeration system is gas expansion refrigeration system or azeotrope refrigeration system;
(3) out knockout drum is entered to afterwards from described heat exchanger package coke-stove gas out;
(4) logistics out of the bottom of described knockout drum enters rectifying column; Logistics at the bottom of described rectifying tower enters to the reboiler be arranged at the bottom of described rectifying tower; From described reboiler, logistics is out again through the throttling of J-T valve, obtains liquefied natural gas;
From the top of described knockout drum, logistics is out through described heat exchanger package rewarming;
Next logistics is ejected through described heat exchanger package rewarming from described rectifying tower;
The logistics of described gas-liquid separation pot bottom enters to described rectifying column from the middle part of described rectifying column;
From described reboiler, logistics out obtains liquefied natural gas through the throttling of J-T valve again after cooling;
In step (2), described coke-stove gas flow B is cooled to-20 DEG C ~-120 DEG C, described cooling procedure provides heat for described reboiler;
-140 DEG C ~-160 DEG C are cooled to through described heat exchanger package after described coke-stove gas material flow A and the mixing of coke-stove gas flow B.
2. method according to claim 1, is characterized in that: logistics out from described reboiler is cooled to-150 DEG C ~-162 DEG C.
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| CN106016968A (en) * | 2016-07-14 | 2016-10-12 | 王嘉文 | Method and device for liquidation purification of carbon dioxide |
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| CN108826830B (en) * | 2018-07-12 | 2024-01-09 | 北京拓首能源科技股份有限公司 | Intermediate feeding coke oven gas recovery system utilizing liquefied natural gas cold energy |
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| CN114061265A (en) * | 2020-08-04 | 2022-02-18 | 杭州中泰深冷技术股份有限公司 | Device and method for large-scale combined production of synthetic ammonia and LNG (liquefied natural gas) by using coke-oven gas |
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