CN105066585B - The purification separation device and method of synthesis gas - Google Patents
The purification separation device and method of synthesis gas Download PDFInfo
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- CN105066585B CN105066585B CN201510514031.3A CN201510514031A CN105066585B CN 105066585 B CN105066585 B CN 105066585B CN 201510514031 A CN201510514031 A CN 201510514031A CN 105066585 B CN105066585 B CN 105066585B
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Abstract
The invention discloses the purification separation device and method of synthesis gas.Wherein, the purification separation device of synthesis gas includes：Heat exchanger group, methane tower reboiler, the second synthesis gas return pipeline, gas-liquid separator, scrubbing tower, the first gas phase pipeline, methane tower, liquid phase pipeline, methane-rich liquid pipeline and the second gas phase pipeline.The device of the invention provides low-temperature receiver without outside, so that it may realize the refined of the synthesis gas containing methane, methane therein is recycled to greatest extent simultaneously, obtains high-purity methane product, and, the structure of device is simple, investment is low with operating cost, and stability is good, and treatment effeciency is high.
Description
Technical field
The present invention relates to chemical fields, and in particular, to the purification separation device and method of synthesis gas.
Background technology
HYGAS gasification technologies are a kind of advanced powdered coal fluidized bed gasification technologies, have that can to handle colm, coproduction light
The characteristics of matter aromatic hydrocarbons and big co-production of methane yield.The characteristics of synthesis gas of HYGAS gasification productions is because rich in methane, is as coal system
The optimal selection of natural gas gasifying technology.And the characteristics of its coal adaptability is strong, coproduction aromatic hydrocarbons, makes it have extensive region and answers
Use advantage.To meet the developing direction of different regions industrial pattern and different user enterprise, by the first in HYGAS gasification synthesis gas
Alkane detaches, and improves synthesis gas (hydrogen+nitrogen mixture or hydrogen+carbon mono oxide mixture) purity, reduces methane therein and contain
Amount makes the unstripped gas of chemosynthesis reaction, produces synthesis of chemicals, is allowed to possess more purposes extremely urgent.It is real
Proof is trampled, if synthesis atmospheric pressure is higher, is not to remove the inert gases such as methane by dry cleaning methods such as pressure-variable adsorptions
Excellent selection.
Therefore, the purification and separation method of the synthesis gas containing methane of high pressure requires study.
Invention content
The present invention is directed at least solve one of technical problem in the prior art.For this purpose, one object of the present invention
It is to propose a kind of device and method of the synthesis gas containing methane using Deep Cooling Method purification coal gasification, qualified synthesis gas is being made
Meanwhile also obtain high-purity methane product.
According to an aspect of the present invention, the present invention provides a kind of purification separation devices of synthesis gas.According to the present invention
Embodiment, including：Heat exchanger group, for carrying out the first heat exchange processing to the synthesis gas, first to be cooled down closes
Into gas；Methane tower reboiler, the methane tower reboiler are connected with the heat exchanger group, for first synthesis gas to be carried out
Cooling is handled, to obtain the second synthesis gas and heat；Second synthesis gas return pipeline, the second synthesis gas return pipeline with
The heat exchanger group is connected with the methane tower reboiler, for second synthesis gas to be delivered to the heat exchanger group, profit
The second heat exchange processing is carried out with the heat exchanger group, to make the methane liquefaction in second synthesis gas, obtains gas-liquid mixed
Object；Gas-liquid separator, the gas-liquid separator are connected with the heat exchanger group, for the gas-liquid mixture to be carried out at separation
Reason, to obtain gas phase and liquid phase；Scrubbing tower, the scrubbing tower are connected with the gas-liquid separator and the heat exchanger group, use
In carrying out carrying out washing treatment to the gas phase, so as to the gas phase after being purified；First gas phase pipeline, the first gas phase pipeline with
The scrubbing tower is connected with the heat exchanger group, for the heat exchanger group, the purified gas-phase transport to be utilized institute
It states heat exchanger group and carries out third heat exchange processing, to obtain the gas phase of re-heat；Methane tower, the methane tower and the gas-liquid separation
Device, the methane tower reboiler, the scrubbing tower are connected with the heat exchanger group, for being carried out at the first rectifying to the liquid phase
Reason, to obtain the liquid phase after rectifying and the gas phase after rectifying；Liquid phase pipeline, the liquid phase pipeline and the methane tower and described
Methane tower reboiler is connected, for the liquid phase after the rectifying to be delivered to the methane tower reboiler, using the heat into
Row heating evaporation and the second rectification process, to obtain methane-rich liquid；Methane-rich liquid pipeline, the methane-rich liquid re-heat
Pipeline is connected with the methane tower reboiler and the heat exchanger group, for the methane-rich liquid to be delivered to the heat exchanger
Group carries out the 4th heat exchange using the heat exchanger group and handles, to obtain methane gas；Second gas phase pipeline, second gas phase
Pipeline is connected with the methane tower and the heat exchanger group, for by the gas-phase transport after the rectifying to the heat exchanger group,
The 5th heat exchange is carried out using the heat exchanger group to handle, to obtain fuel gas.
Device according to embodiments of the present invention provides low-temperature receiver without outside, so that it may realize the refined of the synthesis gas containing methane, together
When recycle methane therein to greatest extent, obtain high-purity methane product, also, the structure of device is simple, investment and operation
At low cost, stability is good, and treatment effeciency is high.
In addition, the purification separation device of synthesis gas according to the above embodiment of the present invention can also have following additional skill
Art feature：
According to an embodiment of the invention, which further comprises：Pretreatment unit, it is pre- for being carried out to the synthesis gas
Processing, removes the impurity in the synthesis gas, so as to the synthesis gas after being purified.
According to an embodiment of the invention, the heat exchanger group includes First Heat Exchanger and the second heat exchanger.
According to an embodiment of the invention, First Heat Exchanger and the second heat exchanger are plate-fin heat exchanger.
According to an embodiment of the invention, the scrubbing tower and methane tower are plate column or packed tower.
According to an embodiment of the invention, the methane tower reboiler is built-in thermosiphon reboiler or external type heat siphon
Reboiler.
According to an embodiment of the invention, the methane tower further comprises：Condenser, the condenser are arranged on the first
The top of alkane tower for carrying out condensation process to the gas phase after the rectifying, condenses the methane in the gas phase after the rectifying
Liquefaction, and flow back and mixed with the methane-rich liquid.According to an embodiment of the invention, the gas-liquid separator and the methane tower
It is attached by expenditure and pressure valve.
According to another aspect of the present invention, the present invention provides a kind of sides using aforementioned device purification separation synthesis gas
Method, the synthesis gas contain methane.According to an embodiment of the invention, this method includes：Using heat exchanger group to the synthesis gas
The first heat exchange processing is carried out, so as to the first synthesis gas cooled down；Using methane tower reboiler by first synthesis gas into
Row cooling is handled, so as to the second synthesis gas and heat after cool down, wherein, the heat is methane tower heat supply；Using changing
Second synthesis gas is carried out the second heat exchange processing by hot device group, makes the methane liquefaction in second synthesis gas, to obtain
Gas-liquid mixture；The gas-liquid mixture is subjected to separating treatment using gas-liquid separator, to obtain gas phase and liquid phase；It utilizes
Scrubbing tower carries out carrying out washing treatment to the gas phase, so as to the gas phase after being purified；Using the heat exchanger group to the purification
Gas phase afterwards carries out third heat exchange processing, to obtain the gas phase of re-heat；The first rectifying is carried out to the liquid phase using methane tower
Processing, to obtain the liquid phase after rectifying and the gas phase after rectifying；The liquid phase after the rectifying is carried out using methane reboil column
Heating evaporation and the second rectification process, to obtain methane-rich liquid；Using the heat exchanger group by the methane-rich liquid into
The 4th heat exchange of row is handled, to obtain the methane gas；And the gas phase after the rectifying is carried out using the heat exchanger group
5th heat exchange is handled, to obtain fuel gas.
According to the method for the embodiment of the present invention, low-temperature receiver is provided without outside, so that it may realize the refined of the synthesis gas containing methane, together
When recycle methane therein to greatest extent, obtain high-purity methane product, also, the easy to operate of this method, investment and fortune
Row is at low cost, and safety is good, and treatment effeciency is high.
According to an embodiment of the invention, this method further comprises：The synthesis gas is pre-processed, removes the conjunction
Into the impurity in gas, so as to the synthesis gas after being purified.
According to an embodiment of the invention, the temperature of first synthesis gas is -100~-140 DEG C；Second synthesis gas
Temperature be -110~-150 DEG C；The temperature of the gas-liquid mixture is -170~-190 DEG C.
The additional aspect and advantage of the present invention will be set forth in part in the description, and will partly become from the following description
It obtains significantly or is recognized by the practice of the present invention.
Description of the drawings
The above-mentioned and/or additional aspect and advantage of the present invention will become in the description from combination accompanying drawings below to embodiment
Significantly and it is readily appreciated that, wherein：
Fig. 1 shows the structure diagram of the purification separation device of synthesis gas according to an embodiment of the invention；
Fig. 2 shows the method flow schematic diagram of purification separation synthesis gas according to an embodiment of the invention.
Specific embodiment
The embodiment of the present invention is described below in detail, the example of the embodiment is shown in the drawings, wherein from beginning to end
Same or similar label represents same or similar element or the element with same or like function.Below with reference to attached
The embodiment of figure description is exemplary, and is only used for explaining the present invention, and is not considered as limiting the invention.
In the description of the present invention, term " longitudinal direction ", " transverse direction ", " on ", " under ", "front", "rear", "left", "right", " perpendicular
Directly ", the orientation of the instructions such as " level ", " top ", " bottom " or position relationship are based on orientation shown in the drawings or position relationship, are only
The present invention rather than require the present invention therefore it is not intended that right with specific azimuth configuration and operation for ease of description
The limitation of the present invention.
It should be noted that term " first ", " second " are only used for description purpose, and it is not intended that instruction or hint phase
To importance or the implicit quantity for indicating indicated technical characteristic.Define " first " as a result, the feature of " second " can be with
Express or implicitly include one or more this feature.Further, in the description of the present invention, unless otherwise saying
Bright, " multiple " are meant that two or more.
According to an aspect of the present invention, the present invention provides a kind of purification separation devices of synthesis gas.With reference to figure 1, root
According to the embodiment of the present invention, the purification separation device of the synthesis gas of the present invention is explained, the direction of arrow is in figure
The direction of material flows, the device include：Heat exchanger group 100, methane tower reboiler 200, the second synthesis gas return pipeline 800,
Gas-liquid separator 300, scrubbing tower 400, the first gas phase pipeline 900, methane tower 500, liquid phase pipeline 1100, methane-rich liquid pipeline
1200 and the second gas phase pipeline 1300, wherein, heat exchanger group 100 is used to carry out the first heat exchange processing to synthesis gas, is cooled down
The first synthesis gas；Methane tower reboiler 200 is connected with heat exchanger group 100, for the first synthesis gas to be carried out cooling processing, obtains
To the second synthesis gas and heat；Second synthesis gas return pipeline 800 is connected with heat exchanger group 100 and methane tower reboiler 200, uses
In the second synthesis gas is delivered to heat exchanger group 100, the second heat exchange processing is carried out using heat exchanger group, is made in the second synthesis gas
Methane liquefaction obtains gas-liquid mixture；Gas-liquid separator 300 is connected with heat exchanger group 100, for gas-liquid mixture to be divided
From processing, gas phase and liquid phase are obtained；Scrubbing tower 400 is connected with gas-liquid separator 300 and heat exchanger group 100, for gas phase into
Row carrying out washing treatment, the gas phase after being purified；First gas phase pipeline 900 is connected with scrubbing tower 400 and heat exchanger group 100, is used for
By purified gas-phase transport to heat exchanger group 100, third heat exchange processing is carried out using heat exchanger group 100, to obtain re-heat
Gas phase；Methane tower 500 is connected with gas-liquid separator 300, methane tower reboiler 200 and heat exchanger group 100, for liquid phase into
The first rectification process of row, obtains the liquid phase after rectifying and the gas phase after rectifying；Liquid phase pipeline 1100 and methane tower 500 and methane tower
Reboiler 200 is connected, and for the liquid phase after rectifying to be delivered to methane tower reboiler 200, is cooled down using the first synthesis gas
The heat that processing generates carries out heating evaporation and the second rectification process, obtains methane-rich liquid, then methane-rich liquid is returned first
Alkane tower 500；Methane-rich liquid pipeline 1200 is connected with methane tower 500 and heat exchanger group 100, for methane-rich liquid to be delivered to
Heat exchanger group 100 carries out the 4th heat exchange using heat exchanger group 100 and handles, obtains methane gas, which is the methane of re-heat
Gas；Second gas phase pipeline 1300 is connected with methane tower 500 and heat exchanger group 100, for the gas-phase transport after rectifying extremely to be exchanged heat
Device group 100 carries out the 5th heat exchange using heat exchanger group 100 and handles, obtains fuel gas, which is the fuel gas of re-heat.
Wherein, it should be noted that containing a plurality of heat exchanger channels in heat exchanger group 100 of the invention, ensure different product
It exchanges heat in different heat exchanger channels, not only heat exchange efficiency is high, but also avoids the pollution between different product.
Device according to embodiments of the present invention, is provided low-temperature receiver without outside, is handled using heat exchange, and deep cooling is carried out to synthesis gas
Separation, realizes the reasonable utilization of the energy, and can be refined to containing methane synthesis gas, while recycle to greatest extent wherein
Methane, obtain high-purity methane product, also, the structure of the device of the invention is simple, invests, stability low with operating cost
Good, treatment effeciency is high.
Term " deep cooling separation " is used in the present invention, " cryogenic separation " represents mixture by using less than operating
Separation method (the example run under the minimum temperature of the temperature required by at least one component of mixture condensation under pressure
As condensed, distilling and/or be fractionated) it is detached.In general, the minimum temperature will be less than -60 ℉ (- 50 DEG C), be preferably lower than -
150℉(-100℃)。
According to an embodiment of the invention, synthesis gas is obtained by coal gasification.Methane content is high in synthesis gas as a result,.
According to an embodiment of the invention, which further comprises：Pretreatment unit 600, for the synthesis gas into
Row pretreatment, removes the impurity in the synthesis gas, so as to the synthesis gas after being purified.As a result, by pretreatment, removal is closed
Into impurity such as moisture content, carbon dioxide and the methanol in gas, and then, obtained fuel gas and the purity higher of methane gas is suitble to cold
Case processing avoids equipment in ice chest from blocking or damage.
According to some embodiments of the present invention, pretreatment unit 600 includes absorber and dust filter unit.According to the present invention
Some embodiments, absorber is molecular sieve adsorber.According to a particular embodiment of the invention, pretreatment unit includes two points
Son sieve, when running for one, synthesis gas enters online molecule cribellum bed, and moisture, carbon dioxide, methanol are when passing through bed
Bed body is inhaled into, another, then in regeneration cycle, cools down and for use, by being heated from nitrogen out-of-bounds by steam heater
After regenerated.Wherein, regeneration is carried out using low-pressure nitrogen or other gases, is heated, is added by regeneration gas steam heater
Low-pressure nitrogen after heat removes moisture, the CO of saturated bed through over-molecular sieve2And the impurity of other absorption, then, regeneration gas exists
Home is vented, meanwhile, the synthesis gas dried through molecular sieve leaves online molecular sieve, by dust filter unit, subsequently into
Ice chest carries out cryogenic purification separating treatment.
According to an embodiment of the invention, heat exchange cooling is carried out to high pressure nitrogen using heat exchanger group 100 to handle, obtains liquid
Nitrogen, the liquid nitrogen are divided into three strands, one carries out synthesis gas washing as the cleaning solution of scrubber overhead 400 and refines；One stock-traders' know-how exchanges heat
Device group enters synthesis gas pipeline, gas phase is carried out to match nitrogen, the volume ratio of nitrogen and hydrogen is (2.8~3.2) in gas phase：1, preferably
Ground is 3:1；One (a small amount of) exports gas phase to methane tower 500 into condenser 510 and cools down, and generates phegma, increases
Add methane gas recovery rate.It is liquefied as a result, by the use of high pressure nitrogen as low-temperature receiver, does not have to provide low-temperature receiver outside device substantially, so that it may real
Now the synthesis gas containing methane is refined, while has recycled methane therein to greatest extent, obtains high-purity methane product.
According to an embodiment of the invention, heat exchanger group 100 includes 110 and second heat exchanger 120 of First Heat Exchanger.As a result,
Heat exchange efficiency is high, and effect is good, especially, carries out that the temperature that heat exchange cools is low, and the effect of cryogenic separation is good to synthesis gas.
According to an embodiment of the invention, 110 and second heat exchanger 120 of First Heat Exchanger is plate-fin heat exchanger.As a result,
Heat exchange efficiency higher, it is better, especially, synthesis gas is carried out heat exchange cool processing temperature it is low, take up an area few, cost
Low, the effect of cryogenic separation is good, and the rate of recovery of methane is high, and obtained fuel gas and the purity of methane gas is high.
According to an embodiment of the invention, scrubbing tower 400 and methane tower 500 are plate column or packed tower.It is washed as a result, in satisfaction
Wash, rectification effect while, according to the size of processing tolerance, 400 He of scrubbing tower is realized in the requirement of operating flexibility, resistance drop etc.
Methane tower 500 uses the optimal combination of corresponding tower.
According to an embodiment of the invention, methane tower reboiler 200 is built-in thermosiphon reboiler or external type heat siphon
Reboiler.The good separating effect of synthesis gas as a result, compact arrangement of equipment difficulty is low, is conducive to the installation cloth of the device of big specification
It puts.
According to an embodiment of the invention, methane tower 500 further comprises：Condenser 510, the condenser are arranged on described
The top of methane tower for carrying out condensation process to the gas phase after the rectifying, makes the methane in the gas phase after the rectifying cold
Lime set, and flow back and mixed with the methane-rich liquid.Condensation process is further carried out to the methane for cryogenic liquefying as a result,
Liquefied methane is obtained, so as to which the rate of recovery of methane is high, and the methane content in fuel gas is low.In addition it is also possible to by scrubbing tower
The partially liq of 400 bottom of towe is back in methane tower 500, and is mixed with methane-rich liquid.As a result, by first liquefied in scrubbing tower
Alkane returns to methane tower, so as to which the rate of recovery of methane is high, and the methane content in fuel gas is low.
According to an embodiment of the invention, gas-liquid separator 300 is gas-liquid separator or flash tank.As a result, fully by liquid phase
It is detached from gas-liquid mixture, liquid phase is avoided to lose.
According to an embodiment of the invention, the gas-liquid separator is connected with the methane tower by expenditure and pressure valve 700
It connects.Throttled as a result, by depressurizing, while lower temperature logistics is obtained, the former nitrogen being dissolved in liquid methane, argon gas,
Carbon monoxide, hydrogen etc. parse, and improve the purity of high methane gas.
According to another aspect of the present invention, the present invention provides a kind of sides using aforementioned device purification separation synthesis gas
Method, the synthesis gas contain methane.With reference to figure 2, according to an embodiment of the invention, which is explained, this method packet
It includes：
The first heat exchange of S100 is handled
According to an embodiment of the invention, the first heat exchange processing is carried out to the synthesis gas using heat exchanger group, is cooled down
The first synthesis gas.The gas for treating re-heat of synthesis gas to be cooled and purification separation purified treatment is carried out at heat exchange as a result,
Reason, cools down synthesis gas, without external source, realizes reasonable, the efficient utilization of energy.Some realities according to the present invention
Example is applied, the temperature of the first synthesis gas is -100~-140 DEG C.
According to an embodiment of the invention, this method further comprises：In the first heat exchange before processing, the synthesis gas is carried out
Pretreatment, removes the impurity in the synthesis gas, and so as to the synthesis gas after being purified, which is suitble to ice chest to handle.By
This, is by pre-processing, the impurity such as moisture content, carbon dioxide and methanol in removal synthesis gas, and then, above-mentioned medium is avoided cold
Accumulation, condensation and occluding device or damage equipment in case.
According to an embodiment of the invention, heat exchange cooling is carried out to high pressure nitrogen using heat exchanger group to handle, obtains liquid nitrogen, it should
Liquid nitrogen is divided into three strands, one carries out synthesis gas washing as the cleaning solution of scrubber overhead 400 and refines；One stock-traders' know-how heat exchanger group into
Enter synthesis gas pipeline, gas phase is carried out to match nitrogen, the volume ratio of nitrogen and hydrogen is (2.8~3.2) in gas phase：1, it is preferable that be
3:1；One (a small amount of) exports condensate liquid to methane tower 500 into condenser 510 and cools, and generates phegma, increases methane
Gas recovery rate.It is liquefied as a result, by the use of high pressure nitrogen as low-temperature receiver, does not have to provide low-temperature receiver outside device substantially, so that it may realize containing first
Refining, while recycled methane therein to greatest extent for alkane synthesis gas, obtains high-purity methane product.
S200 coolings are handled
According to an embodiment of the invention, the first synthesis gas is subjected to cooling processing using methane tower reboiler.Cooled down
The second synthesis gas and heat afterwards, wherein, which is methane tower heat supply.It is released as a result, using the first synthesis gas in cooling processing
The heat put is methane tower heat supply, realizes reasonable, the efficient utilization of energy.According to some embodiments of the present invention, described
The temperature of two synthesis gas is -110~-150 DEG C.
The second heat exchange of S300 is handled
According to an embodiment of the invention, the second synthesis gas is subjected to the second heat exchange processing using heat exchanger group, makes the second conjunction
Into the methane liquefaction in gas, gas-liquid mixture is obtained.Heat exchanger group is reused as a result, and carries out heat exchange cooling processing, utilizes first
The condensing temperature of alkane and other gases is poor, makes the methane liquefaction in the second synthesis gas.According to some embodiments of the present invention, gas-liquid
The temperature of mixture is -170~-190 DEG C.
S400 separating treatments
According to an embodiment of the invention, gas-liquid mixture is subjected to separating treatment using gas-liquid separator, to obtain gas
Phase and liquid phase.As a result, from the isolated liquid phase of gas-liquid mixture, which is methane.
S500 carrying out washing treatment
According to an embodiment of the invention, carrying out washing treatment is carried out to the gas phase using scrubbing tower, after being purified
Gas phase.The purity of gas phase is high as a result,.
According to some embodiments of the present invention, gas phase contains nitrogen and hydrogen, and hydrogen：The volume ratio of nitrogen is more than 3:1.
According to some embodiments of the present invention, carrying out washing treatment is carried out using liquid nitrogen.The purity of gas phase is high as a result, and does not draw
Enter impurity, and nitrogen is added into gas phase, make in gas phase the volume ratio of nitrogen and hydrogen close to 1：3.
The heat exchange of S600 thirds is handled
According to an embodiment of the invention, third heat exchange processing is carried out to purified gas phase using heat exchanger group, is answered
The gas phase of heat.Re-heat is carried out to gas phase by heat exchange to gas phase using the synthesis gas to be cooled of room temperature as a result, realizes energy
Rationally, it efficiently utilizes.
According to some embodiments of the present invention, third heat exchange processing is being carried out to purified gas phase using heat exchanger group
When, distribution can be carried out to the gas phase using the nitrogen of other channels in the heat exchanger group, the volume ratio for making nitrogen and hydrogen is
(2.8~3.2)：1, it is preferable that be 3:1.
The first rectification process of S700
According to an embodiment of the invention, the first rectification process is carried out to liquid phase using methane tower, obtains the liquid phase after rectifying
With the gas phase after rectifying.The purity higher of liquid and gas as a result, and then methane gas and the purity higher of fuel gas.
S800 heating evaporations and the second rectification process
According to an embodiment of the invention, the liquid phase after the rectifying is subjected to heating evaporation and second using methane reboiler
Rectification process, to obtain methane-rich liquid.Liquid phase is further purified as a result, methane content in obtained methane-rich liquid
Higher.
According to some embodiments of the present invention, methane content is not less than 96% in methane-rich liquid.
The 4th heat exchange of S900 is handled
According to an embodiment of the invention, methane-rich liquid is carried out the 4th heat exchange using heat exchanger group to handle, to obtain
Methane gas, the methane gas are the methane gas of re-heat.Pass through heat exchange to methane-rich liquid using the synthesis gas to be cooled of room temperature as a result,
Device group carries out re-heat, obtains the methane gas of room temperature, realizes reasonable, the efficient utilization of energy.
The 5th heat exchange of S1000 is handled
According to an embodiment of the invention, the gas phase after the rectifying is carried out at the 5th heat exchange using the heat exchanger group
Reason, to obtain fuel gas, which is the fuel gas of re-heat.Gas phase is led to using the synthesis gas to be cooled of room temperature as a result,
It crosses heat exchanger group and carries out re-heat, obtain the fuel gas of room temperature, realize reasonable, the efficient utilization of energy.
According to some embodiments of the present invention, the gas phase after rectifying includes nitrogen, methane, hydrogen and carbon monoxide.
According to the method for the embodiment of the present invention, low-temperature receiver is provided without outside, so that it may realize the refined of the synthesis gas containing methane, together
When recycle methane therein to greatest extent, obtain high-purity methane product, also, the easy to operate of this method, investment and fortune
Row is at low cost, and safety is good, and treatment effeciency is high.
According to an embodiment of the invention, this method further comprises：The synthesis gas is pre-processed, removes the conjunction
Into the impurity in gas, so as to the synthesis gas after being purified, which is suitble to ice chest to handle.
According to an embodiment of the invention, the temperature of first synthesis gas is -100~-140 DEG C；Second synthesis gas
Temperature be -110~-150 DEG C；The temperature of the gas-liquid mixture is -170~-190 DEG C.
Below with reference to specific embodiment, the present invention will be described, it should be noted that these embodiments are only explanation
Property, and be not considered as limiting the invention.
Embodiment 1
Purification separation processing is carried out to the synthesis gas of coal gasification, and utilize and detach using the purification separation device of synthesis gas
The hydrogen nitrogen ammonia synthesis arrived, wherein, the component of the synthesis gas of the coal gasification is：Hydrogen 78%, methane 19%, nitrogen
0.1%th, carbon monoxide 2%, argon gas 0.1% and ethane 1%.Meanwhile by deep cooling and the method for scrubbing with liquid nitrogen to coal gasification
Synthesis gas carries out refined and obtains high-purity methane product, wherein, the structure of purification separation device is as shown in Figure 1, utilize the dress
It is as follows to put the step of purification separation processing is carried out to synthesis gas：
(1) synthesis gas is pre-processed using pretreatment unit, removes moisture, carbon dioxide, methanol in synthesis gas
With the impurity such as dust, the synthesis gas of dry suitable ice chest processing is obtained.
(2) dry synthesis gas enters 110 channel B3 of heat exchanger, and temperature is down to -110~-140 DEG C.Meanwhile high pressure nitrogen
(pressure is combined to atmospheric pressure higher than Import Gas) passes sequentially through 120 channel A5 of heat exchanger, 110 channel B6 of heat exchanger, temperature drop
To -170~-190 DEG C, liquefaction of nitrogen is liquid nitrogen, wherein, fraction liquid nitrogen enters scrubbing tower as washing column overhead cleaning solution
400, most of liquid nitrogen is incorporated a certain amount of nitrogen when synthesis gas passes through heat exchanger 110 by channel B8, becomes qualified hydrogen nitrogen
Synthesis gas is sent out, and small part liquid nitrogen enters methane tower 500 as refrigerant and pushes up condenser 510, and cold is provided to overhead condenser 510
Afterwards, by 110 channel B1 of heat exchanger, 120 channel A1 re-heats of heat exchanger air is discharged into after room temperature.
(3) synthesis gas that step (2) obtains enters methane tower reboiler 200, and evaporation heat is provided to methane tower 500, itself
- 120~-150 DEG C are cooled to, subsequently enters the channel B7 of heat exchanger 110, temperature is down to -170~-190 DEG C, gasifies at this time
Most methane liquefactions, obtains gas-liquid mixed media in synthesis gas.
(4) gas-liquid mixed media enters 300 centre entrance of knockout drum, and the upper end outlet of knockout drum 300 is with washing
The connection of 400 lower entrances of tower is washed, the gas phase that knockout drum 300 is isolated enters scrubbing tower 400, essence is obtained by scrubbing with liquid nitrogen
Purified gas (H processed2：N2Volume ratio is more than 3:1), fine gas is normal by 110 channel B5 of heat exchanger, 120 channel A4 re-heats of heat exchanger
Temperature when synthesis gas passes through heat exchanger 110, is incorporated a certain amount of nitrogen by channel B8, becomes qualified hydrogen nitrogen synthesis gas (12)
It sends out, wherein, H2 in hydrogen nitrogen synthesis gas：N2 volume ratio=3:1.
(5) the lower end outlet of knockout drum 300 is connected by expenditure and pressure valve 700 with 500 middle part of methane tower, gas-liquid point
From the liquid in tank 300 by throttling, into methane tower 500, heating evaporation and rectifying point by methane tower reboiler 200
From obtaining the very high methane-rich liquid of purity in 500 bottom of methane tower, CH4% ＞ 96% in the methane-rich liquid.
(6) 500 bottom liquid methane of methane tower is after throttle valve 700 depressurizes throttling expansion, by 110 channel of heat exchanger
It is sent outside after after B4,120 channel A3 re-heats to room temperature of heat exchanger as methane gas product, in methane gas product, methane+ethane >=
98%.
(7) gas phase at 500 top of methane tower exchanges heat through overhead condenser 510, and partial gas phase liquefaction is flowed back to as phegma
500 tower top of methane tower.500 top fixed gas of methane tower is through 110 channel B2 of heat exchanger, 120 channel A2 re-heats of heat exchanger into room temperature
It is sent outside afterwards as fuel gas, methane content is less than 1% in the fuel gas component.
In the description of this specification, reference term " one embodiment ", " example ", " is specifically shown " some embodiments "
The description of example " or " some examples " etc. means specific features, structure, material or the spy for combining the embodiment or example description
Point is contained at least one embodiment of the present invention or example.In the present specification, schematic expression of the above terms are not
Centainly refer to identical embodiment or example.Moreover, particular features, structures, materials, or characteristics described can be any
One or more embodiments or example in combine in an appropriate manner.
Although an embodiment of the present invention has been shown and described, it will be understood by those skilled in the art that：Not
In the case of being detached from the principle of the present invention and objective a variety of change, modification, replacement and modification can be carried out to these embodiments, this
The range of invention is limited by claim and its equivalent.
Claims (14)
1. a kind of purification separation device of synthesis gas, the synthesis gas contain methane, which is characterized in that including：
Heat exchanger group, for carrying out the first heat exchange processing to the synthesis gas, so as to the first synthesis gas cooled down；
Methane tower reboiler, the methane tower reboiler are connected with the heat exchanger group, for first synthesis gas to be carried out
Cooling is handled, to obtain the second synthesis gas and heat；
Second synthesis gas return pipeline, the second synthesis gas return pipeline and the heat exchanger group and the methane tower reboiler
It is connected, for second synthesis gas to be delivered to the heat exchanger group, the second heat exchange processing is carried out using the heat exchanger group,
To make the methane liquefaction in second synthesis gas, gas-liquid mixture is obtained；
Gas-liquid separator, the gas-liquid separator are connected with the heat exchanger group, for the gas-liquid mixture to be detached
Processing, to obtain gas phase and liquid phase；
Scrubbing tower, the scrubbing tower are connected with the gas-liquid separator and the heat exchanger group, for being washed to the gas phase
Processing is washed, so as to the gas phase after being purified；
First gas phase pipeline, the first gas phase pipeline are connected with the scrubbing tower and the heat exchanger group, for will be described net
Gas-phase transport after change carries out third heat exchange processing, to obtain re-heat to the heat exchanger group using the heat exchanger group
Gas phase；Methane tower, the methane tower and the gas-liquid separator, the methane tower reboiler, the scrubbing tower and the heat exchange
Device group is connected, for carrying out the first rectification process to the liquid phase, to obtain the liquid phase after rectifying and the gas phase after rectifying；
Liquid phase pipeline, the liquid phase pipeline are connected with the methane tower and the methane tower reboiler, for will be after the rectifying
Liquid phase be delivered to the methane tower reboiler, heating evaporation and the second rectification process are carried out using the heat, to obtain
Methane-rich liquid, then the methane-rich liquid is returned into the methane tower；
Methane-rich liquid pipeline, the methane-rich liquid pipeline are connected with the methane tower and the heat exchanger group, for by institute
It states methane-rich liquid and is delivered to the heat exchanger group, carrying out the 4th heat exchange using the heat exchanger group is handled, to obtain methane
Gas；And
Second gas phase pipeline, the second gas phase pipeline are connected with the methane tower and the heat exchanger group, for by the essence
Gas-phase transport after evaporating carries out the 5th heat exchange using the heat exchanger group and handles, to obtain fuel gas to the heat exchanger group.
2. the apparatus according to claim 1, which is characterized in that further comprise：
Pretreatment unit for being pre-processed to the synthesis gas, removes the impurity in the synthesis gas, to be purified
Synthesis gas afterwards.
3. the apparatus according to claim 1, which is characterized in that the heat exchanger group includes First Heat Exchanger and the second heat exchange
Device.
4. device according to claim 3, which is characterized in that the First Heat Exchanger and second heat exchanger are plate
Fin heat exchanger.
5. the apparatus according to claim 1, which is characterized in that the scrubbing tower and methane tower are plate column or packed tower.
6. the apparatus according to claim 1, which is characterized in that the methane tower reboiler is built-in thermosiphon reboiler
Or external thermosiphon reboiler.
7. the apparatus according to claim 1, which is characterized in that the methane tower further comprises：
Condenser, the condenser are arranged on the top of the methane tower, for being carried out at condensation to the gas phase after the rectifying
Reason makes the methane condensation liquefaction in the gas phase after the rectifying, and flows back and mixed with the methane-rich liquid.
8. the apparatus according to claim 1, which is characterized in that the gas-liquid separator is subtracted with the methane tower by throttling
Pressure valve is attached.
9. a kind of method using claim 1~8 any one of them device purification separation synthesis gas, the synthesis gas contains
Methane, which is characterized in that including：
The first heat exchange processing is carried out to the synthesis gas using heat exchanger group, so as to the first synthesis gas cooled down；
First synthesis gas is subjected to cooling processing using methane tower reboiler, so as to the second synthesis gas after being cooled down and
Heat, wherein, the heat is methane tower heat supply；
Second synthesis gas is subjected to the second heat exchange processing using heat exchanger group, makes the methane liquid in second synthesis gas
Change, to obtain gas-liquid mixture；
The gas-liquid mixture is subjected to separating treatment using gas-liquid separator, to obtain gas phase and liquid phase；
Carrying out washing treatment is carried out to the gas phase using scrubbing tower, so as to the gas phase after being purified；
Third heat exchange processing is carried out to the purified gas phase using the heat exchanger group, to obtain the gas phase of re-heat；
The first rectification process is carried out to the liquid phase using methane tower, to obtain the liquid phase after rectifying and the gas phase after rectifying；
The liquid phase after the rectifying is subjected to heating evaporation and the second rectification process using methane reboiler, to obtain methane rich
Liquid；
The methane-rich liquid is carried out the 4th heat exchange using the heat exchanger group to handle, to obtain the methane gas；And
The gas phase after the rectifying is carried out the 5th heat exchange using the heat exchanger group to handle, to obtain fuel gas.
10. according to the method described in claim 9, it is characterized in that, further comprise
The 6th heat exchange is carried out using the heat exchanger group to high pressure nitrogen to handle, to obtain liquid nitrogen；
The carrying out washing treatment is carried out using a part for the liquid nitrogen, so as to the gas phase after being purified；
The another part of the liquid nitrogen is added in the purified gas phase, to obtain with nitrogen phase, wherein, it is described to match nitrogen
The volume ratio of hydrogen and nitrogen is (2.8~3.2) in gas phase：1；And
Condensation process is carried out to the gas phase after the rectifying using a part again for the liquid nitrogen, to make the gas after the rectifying
Methane condensation liquefaction in phase, and flow back and mixed with the methane-rich liquid.
11. according to the method described in claim 10, it is characterized in that, described be with the volume ratio of hydrogen and nitrogen in nitrogen phase
3：1.
12. according to the method described in claim 10, it is characterized in that, the partially liq of the scrubbing tower bottom of towe is back to institute
It states in methane tower, and is mixed with the methane-rich liquid.
13. according to the method described in claim 9, it is characterized in that, further comprise：
The synthesis gas is pre-processed, removes the impurity in the synthesis gas, so as to the synthesis gas after being purified.
14. according to the method described in claim 9, it is characterized in that,
The temperature of first synthesis gas is -100~-140 DEG C；
The temperature of second synthesis gas is -110~-150 DEG C；
The temperature of the gas-liquid mixture is -170~-190 DEG C.
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| CN109678111A (en) * | 2017-10-19 | 2019-04-26 | 无锡佳龙换热器股份有限公司 | Hydrogen purification heat exchanger |
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| EP0933330A2 (en) * | 1998-02-02 | 1999-08-04 | Air Products And Chemicals, Inc. | Separation of carbon monoxide from nitrogen-contaminated gaseous mixtures also containing hydrogen |
| US6062042A (en) * | 1998-01-13 | 2000-05-16 | Air Products And Chemicals, Inc. | Seperation of carbon monoxide from nitrogen-contaminated gaseous mixtures |
| DE102006051759A1 (en) * | 2006-11-02 | 2008-05-08 | Linde Ag | Process and apparatus for decomposing synthesis gas by means of methane scrubbing |
| CN101476813A (en) * | 2009-01-21 | 2009-07-08 | 四川空分设备(集团)有限责任公司 | Feed gas separation method and apparatus of coal gasification apparatus |
| CN101874186A (en) * | 2007-03-20 | 2010-10-27 | 林德股份公司 | Method and device for obtaining gaseous products and liquid methane from synthesis gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6062042A (en) * | 1998-01-13 | 2000-05-16 | Air Products And Chemicals, Inc. | Seperation of carbon monoxide from nitrogen-contaminated gaseous mixtures |
| EP0933330A2 (en) * | 1998-02-02 | 1999-08-04 | Air Products And Chemicals, Inc. | Separation of carbon monoxide from nitrogen-contaminated gaseous mixtures also containing hydrogen |
| DE102006051759A1 (en) * | 2006-11-02 | 2008-05-08 | Linde Ag | Process and apparatus for decomposing synthesis gas by means of methane scrubbing |
| CN101874186A (en) * | 2007-03-20 | 2010-10-27 | 林德股份公司 | Method and device for obtaining gaseous products and liquid methane from synthesis gas |
| CN101476813A (en) * | 2009-01-21 | 2009-07-08 | 四川空分设备(集团)有限责任公司 | Feed gas separation method and apparatus of coal gasification apparatus |
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