CN105066585A - Purifying and separating device and method for synthesis gas - Google Patents
Purifying and separating device and method for synthesis gas Download PDFInfo
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- CN105066585A CN105066585A CN201510514031.3A CN201510514031A CN105066585A CN 105066585 A CN105066585 A CN 105066585A CN 201510514031 A CN201510514031 A CN 201510514031A CN 105066585 A CN105066585 A CN 105066585A
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Abstract
The invention discloses a purifying and separating device and method for synthesis gas. The purifying and separating device for the synthesis gas comprises a heat exchanger set, a methane tower reboiler, a second synthesis gas return pipeline, a gas-liquid separator, a washing tower, a first gas phase pipeline, a methane tower, a liquid phase pipeline, a methane-rich liquid pipeline and a second gas phase pipeline. According to the device, refining of the synthesis gas containing methane can be achieved without an externally provided cold source, meanwhile, the methane in the synthesis gas can be recovered to the greatest extent, and high-purity methane products are obtained; in addition, the device is simple in structure, low in investment and operation cost, good in stability and high in treatment efficiency.
Description
Technical field
The present invention relates to chemical field, particularly, relate to the purification separation apparatus and method of synthesis gas.
Background technology
HYGAS gasification technology is the powdered coal fluidized bed gasification technology of a kind of advanced person, has and can process the large feature of colm, coproduction light aromatics and co-production of methane output.The synthesis gas that HYGAS gasification is produced, because being rich in the feature of methane, is the optimal selection as coal preparing natural gas gasification technology.And its coal adaptability feature that is strong, coproduction aromatic hydrocarbons makes it have extensive region application advantage.For meeting the developing direction of different regions industrial pattern and different user enterprise, by the methane separation in HYGAS gasification synthesis gas, improve synthesis gas (hydrogen+nitrogen mixture or hydrogen+carbon mono oxide mixture) purity, reduce methane content wherein, make it the unstripped gas becoming chemosynthesis reaction, produce synthesis of chemicals, make it to have more purposes extremely urgent.Facts have proved, if synthesis gas pressure is higher, remove the not excellent selection of the inert gases such as methane by dry cleaning methods such as pressure-variable adsorptions.
Therefore, the purification and separation method of the synthesis gas containing methane of high pressure requires study.
Summary of the invention
The present invention is intended at least to solve one of technical problem existed in prior art.For this reason, one object of the present invention is to propose a kind of apparatus and method containing methane synthesis gas utilizing Deep Cooling Method to purify coal gasification, while obtained qualified synthesis gas, also obtain high-purity methane product.
According to an aspect of the present invention, the invention provides a kind of purification separation device of synthesis gas.According to embodiments of the invention, comprising: heat exchanger package, for carrying out the first heat exchange process to described synthesis gas, to obtain the first synthesis gas cooled; Methane tower reboiler, described methane tower reboiler is connected with described heat exchanger package, for described first synthesis gas being carried out cooling process, to obtain the second synthesis gas and heat; Second synthesis gas return pipeline, described second synthesis gas return pipeline is connected with described methane tower reboiler with described heat exchanger package, for described second synthesis gas is delivered to described heat exchanger package, described heat exchanger package is utilized to carry out the second heat exchange process, to make the methane liquefaction in described second synthesis gas, obtain gas-liquid mixture; Gas-liquid separator, described gas-liquid separator is connected with described heat exchanger package, for described gas-liquid mixture is carried out separating treatment, to obtain gas phase and liquid phase; Scrubbing tower, described scrubbing tower is connected with described heat exchanger package with described gas-liquid separator, for carrying out carrying out washing treatment to described gas phase, so that the gas phase after being purified; First gas phase pipeline, described first gas phase pipeline is connected with described heat exchanger package with described scrubbing tower, for by the extremely described heat exchanger package of the gas-phase transport after described purification, utilizes described heat exchanger package to carry out the 3rd heat exchange process, to obtain the gas phase of re-heat; Methane tower, described methane tower is connected with described heat exchanger package with described gas-liquid separator, described methane tower reboiler, described scrubbing tower, for carrying out the first rectification process to described liquid phase, to obtain the gas phase after the liquid phase after rectifying and rectifying; Liquid phase pipeline, described liquid phase pipeline is connected with described methane tower reboiler with described methane tower, for the liquid phase after described rectifying being delivered to described methane tower reboiler, described heat is utilized to carry out heating evaporation and the second rectification process, to obtain methane-rich liquid; Methane-rich liquid pipeline, described methane-rich liquid re-heat pipeline is connected with described heat exchanger package with described methane tower reboiler, for described methane-rich liquid is delivered to described heat exchanger package, described heat exchanger package is utilized to carry out the 4th heat exchange process, to obtain methane gas; Second gas phase pipeline, described second gas phase pipeline is connected with described heat exchanger package with described methane tower, for by the extremely described heat exchanger package of the gas-phase transport after described rectifying, utilizes described heat exchanger package to carry out the 5th heat exchange process, to obtain fuel gas.
According to the device of the embodiment of the present invention, provide low-temperature receiver without the need to outside, just can realize refining containing methane synthesis gas, reclaim methane wherein simultaneously to greatest extent, obtain high-purity methane product, and, the structure of device is simple, investment and operating cost low, good stability, 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 technical characteristic:
According to embodiments of the invention, this device comprises further: pretreatment unit, for carrying out pretreatment to described synthesis gas, removes the impurity in described synthesis gas, so that the synthesis gas after being purified.
According to embodiments of the invention, described heat exchanger package comprises First Heat Exchanger and the second heat exchanger.
According to embodiments of the invention, First Heat Exchanger and the second heat exchanger are plate-fin heat exchanger.
According to embodiments of the invention, described scrubbing tower and methane tower are plate column or packed tower.
According to embodiments of the invention, described methane tower reboiler is built-in thermosiphon reboiler or external thermosiphon reboiler.
According to embodiments of the invention, described methane tower comprises further: condenser, and described condenser is arranged on the top of described methane tower, for carrying out condensation process to the gas phase after described rectifying, make the methane condensation liquefaction in the gas phase after described rectifying, and backflow mixes with described methane-rich liquid.According to embodiments of the invention, described gas-liquid separator is connected by expenditure and pressure valve with described methane tower.
According to a further aspect in the invention, the invention provides a kind of method utilizing aforesaid device purification separation synthesis gas, described synthesis gas contains methane.According to embodiments of the invention, the method comprises: utilize heat exchanger package to carry out the first heat exchange process to described synthesis gas, to obtain the first synthesis gas cooled; Utilize methane tower reboiler described first synthesis gas to be carried out cooling process, to obtain the second synthesis gas after lowering the temperature and heat, wherein, described heat is the heat supply of methane tower; Utilize heat exchanger package that described second synthesis gas is carried out the second heat exchange process, make the methane liquefaction in described second synthesis gas, to obtain gas-liquid mixture; Utilize gas-liquid separator that described gas-liquid mixture is carried out separating treatment, to obtain gas phase and liquid phase; Scrubbing tower is utilized to carry out carrying out washing treatment to described gas phase, so that the gas phase after being purified; Described heat exchanger package is utilized to carry out the 3rd heat exchange process to the gas phase after described purification, to obtain the gas phase of re-heat; Methane tower is utilized to carry out the first rectification process to described liquid phase, to obtain the gas phase after the liquid phase after rectifying and rectifying; The methane tower that boils again is utilized the liquid phase after described rectifying to be carried out heating evaporation and the second rectification process, to obtain methane-rich liquid; Utilize described heat exchanger package that described methane-rich liquid is carried out the 4th heat exchange process, to obtain described methane gas; And utilize described heat exchanger package the gas phase after described rectifying to be carried out the 5th heat exchange process, to obtain fuel gas.
According to the method for the embodiment of the present invention, provide low-temperature receiver without the need to outside, just can realize refining containing methane synthesis gas, reclaim methane wherein simultaneously to greatest extent, obtain high-purity methane product, and, the method simple to operate, investment and operating cost low, security is good, and treatment effeciency is high.
According to embodiments of the invention, the method comprises further: carry out pretreatment to described synthesis gas, removes the impurity in described synthesis gas, so that the synthesis gas after being purified.
According to embodiments of the invention, the temperature of described first synthesis gas is-100 ~-140 DEG C; The temperature of described second synthesis gas is-110 ~-150 DEG C; The temperature of described gas-liquid mixture is-170 ~-190 DEG C.
Additional aspect of the present invention and advantage will part provide in the following description, and part will become obvious from the following description, or be recognized by practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or additional aspect of the present invention and advantage will become obvious and easy understand from accompanying drawing below combining to the description of embodiment, wherein:
Fig. 1 shows the structural representation 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.
Detailed description of the invention
Be described below in detail embodiments of the invention, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Being exemplary below by the embodiment be described with reference to the drawings, only for explaining the present invention, and can not limitation of the present invention being interpreted as.
In describing the invention, term " longitudinal direction ", " transverse direction ", " on ", D score, "front", "rear", "left", "right", " vertically ", " level ", " top ", the orientation of the instruction such as " end " or position relationship be based on orientation shown in the drawings or position relationship, be only the present invention for convenience of description instead of require that the present invention with specific azimuth configuration and operation, therefore must can not be interpreted as limitation of the present invention.
It should be noted that, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise one or more these features.Further, in describing the invention, except as otherwise noted, the implication of " multiple " is two or more.
According to an aspect of the present invention, the invention provides a kind of purification separation device of synthesis gas.With reference to figure 1, according to embodiments of the invention, the purification separation device of synthesis gas of the present invention is explained, in figure, the direction of arrow is the direction of material flows, this device comprises: heat exchanger package 100, methane tower reboiler 200, second synthesis gas return pipeline 800, gas-liquid separator 300, scrubbing tower 400, 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 package 100, for carrying out the first heat exchange process to synthesis gas, obtains the first synthesis gas cooled; Methane tower reboiler 200 is connected with heat exchanger package 100, for the first synthesis gas being carried out cooling process, obtains the second synthesis gas and heat; Second synthesis gas return pipeline 800 is connected with methane tower reboiler 200 with heat exchanger package 100, for the second synthesis gas is delivered to heat exchanger package 100, utilize heat exchanger package to carry out the second heat exchange process, make the methane liquefaction in the second synthesis gas, obtain gas-liquid mixture; Gas-liquid separator 300 is connected with heat exchanger package 100, for gas-liquid mixture is carried out separating treatment, obtains gas phase and liquid phase; Scrubbing tower 400 is connected with heat exchanger package 100 with gas-liquid separator 300, for carrying out carrying out washing treatment to gas phase, and the gas phase after being purified; First gas phase pipeline 900 is connected with heat exchanger package 100 with scrubbing tower 400, for by purification after gas-phase transport to heat exchanger package 100, utilize heat exchanger package 100 to carry out the 3rd heat exchange process, to obtain the gas phase of re-heat; Methane tower 500 is connected with heat exchanger package 100 with gas-liquid separator 300, methane tower reboiler 200, for carrying out the first rectification process to liquid phase, obtains the gas phase after the liquid phase after rectifying and rectifying; Liquid phase pipeline 1100 is connected with methane tower reboiler 200 with methane tower 500, for the liquid phase after rectifying is delivered to methane tower reboiler 200, the heat utilizing the first synthesis gas to carry out cooling process generation carries out heating evaporation and the second rectification process, obtain methane-rich liquid, then methane-rich liquid is returned methane tower 500; Methane-rich liquid pipeline 1200 is connected with heat exchanger package 100 with methane tower 500, for methane-rich liquid is delivered to heat exchanger package 100, utilizes heat exchanger package 100 to carry out the 4th heat exchange process, and obtain methane gas, this methane gas is the methane gas of re-heat; Second gas phase pipeline 1300 is connected with heat exchanger package 100 with methane tower 500, for by the gas-phase transport after rectifying to heat exchanger package 100, utilize heat exchanger package 100 to carry out the 5th heat exchange process, obtain fuel gas, this fuel gas is the fuel gas of re-heat.
Wherein, it should be noted that, containing many heat exchanger channels in heat exchanger package 100 of the present invention, ensure that different product carries out heat exchange in different heat exchanger channels, not only heat exchange efficiency is high, and avoids the pollution between different product.
According to the device of the embodiment of the present invention, there is provided low-temperature receiver without the need to outside, utilize heat exchange process, cryogenic separation is carried out to synthesis gas, realize the Appropriate application of the energy, and can refine containing methane synthesis gas, reclaim methane wherein simultaneously to greatest extent, obtain high-purity methane product, and, the structure of device of the present invention is simple, investment and operating cost low, good stability, treatment effeciency is high.
Use term " deep cooling separation " in the present invention, " cryogenic separation " represent mixture pass through use be separated lower than the separation method (such as condensation, distillation and/or fractionation) carrying out running under operating pressure from the minimum temperature of the temperature required by this mixture condensation at least one component.Usually, described minimum temperature lower than-60 ℉ (-50 DEG C), will be preferably lower than-150 ℉ (-100 DEG C).
According to embodiments of the invention, synthesis gas is obtained by coal gasification.Thus, in synthesis gas, methane content is high.
According to embodiments of the invention, this device comprises further: pretreatment unit 600, for carrying out pretreatment to described synthesis gas, removes the impurity in described synthesis gas, so that the synthesis gas after being purified.Thus, by pretreatment, remove the impurity such as moisture content, carbon dioxide and the methyl alcohol in synthesis gas, and then, the fuel gas obtained and the purity of methane gas higher, be applicable to ice chest process, avoid in ice chest equipment blocking or damage.
According to some embodiments of the present invention, pretreatment unit 600 comprises absorber and dust filter unit.According to some embodiments of the present invention, absorber is molecular sieve adsorber.According to a particular embodiment of the invention, pretreatment unit comprises two molecular sieves, when running for one, synthesis gas enters online molecule cribellum bed, moisture, carbon dioxide, methyl alcohol etc. are by being inhaled into a body during bed, another is then in regeneration cycle, cooling and stand-by, regenerate after being heated by steam heater from nitrogen out-of-bounds.Wherein, regeneration uses low-pressure nitrogen or other gas to carry out, and through the heating of regeneration gas steam heater, the low-pressure nitrogen after heating, through molecular sieve, removes moisture, the CO of saturated bed
2and the impurity of other absorption, then, regeneration gas is in home emptying, and meanwhile, the synthesis gas through molecular sieve drying leaves online molecular sieve, through dust filter unit, then enters ice chest and carries out cryogenic purification separating treatment.
According to embodiments of the invention, utilize heat exchanger package 100 pairs of high pressure nitrogens to carry out heat exchange cooling process, obtain liquid nitrogen, this liquid nitrogen is divided into three strands, and one cleaning solution as scrubber overhead 400 carries out washing to synthesis gas and refines; One stock-traders' know-how heat exchanger package enters synthesis gas pipeline, joins nitrogen to gas phase, and in gas phase, the volume ratio of nitrogen and hydrogen is (2.8 ~ 3.2): 1, preferably, is 3:1; One (on a small quantity) enters condenser 900 pairs of methane towers 500 and exports gas phase and cool, and produces phegma, increases the methane gas rate of recovery.Thus, utilize high pressure nitrogen to liquefy as low-temperature receiver, substantially provide low-temperature receiver without device outside, just can realize refining containing methane synthesis gas, reclaimed methane wherein to greatest extent simultaneously, obtained high-purity methane product.
According to embodiments of the invention, heat exchanger package 100 comprises First Heat Exchanger 110 and the second heat exchanger 120.Thus, heat exchange efficiency is high, effective, especially, carries out the temperature that heat exchange cools low to synthesis gas, cryogenic separation effective.
According to embodiments of the invention, First Heat Exchanger 110 and the second heat exchanger 120 are plate-fin heat exchanger.Thus, heat exchange efficiency is higher, and effect is better, and especially, carry out the cool temperature of process of heat exchange to synthesis gas low, take up an area few, cost is low, cryogenic separation effective, and the rate of recovery of methane is high, the fuel gas obtained and the purity of methane gas high.
According to embodiments of the invention, scrubbing tower 400 and methane tower 500 are plate column or packed tower.Thus, while satisfied washing, rectification effect, according to the size of process tolerance, the requirement of operating flexibility, resistance degradation, realizes the best of breed that scrubbing tower 400 and methane tower 500 adopt corresponding tower.
According to embodiments of the invention, methane tower reboiler 200 is built-in thermosiphon reboiler or external thermosiphon reboiler.Thus, the good separating effect of synthesis gas, compact arrangement of equipment difficulty is low, is conducive to the mounting arrangements of the device of large gauge.
According to embodiments of the invention, methane tower 500 comprises further: condenser 510, described condenser is arranged on the top of described methane tower, for carrying out condensation process to the gas phase after described rectifying, make the methane condensation liquefaction in the gas phase after described rectifying, and backflow mixes with described methane-rich liquid.Thus, carry out condensation process further to the methane for cryogenic liquefying, obtain the methane liquefied, thus the rate of recovery of methane is high, the methane content in fuel gas is low.In addition, also the partially liq at the bottom of scrubbing tower 400 tower can be back in methane tower 500, and mix with methane-rich liquid.Thus, the methane liquefied in scrubbing tower is returned methane tower, thus the rate of recovery of methane is high, the methane content in fuel gas is low.
According to embodiments of the invention, gas-liquid separator 300 is gas-liquid separator or flash tank.Thus, fully liquid phase is separated from gas-liquid mixture, avoids liquid phase to lose.
According to embodiments of the invention, described gas-liquid separator is connected by expenditure and pressure valve 700 with described methane tower.Thus, by decompression throttling, while the logistics of acquisition lower temperature, the former nitrogen be dissolved in liquid methane, argon gas, carbon monoxide, hydrogen etc. parse, and improve the purity of high methane gas.
According to a further aspect in the invention, the invention provides a kind of method utilizing aforesaid device purification separation synthesis gas, described synthesis gas contains methane.With reference to figure 2, according to embodiments of the invention, explain this method, the method comprises:
S100 first heat exchange process
According to embodiments of the invention, utilize heat exchanger package to carry out the first heat exchange process to described synthesis gas, obtain the first synthesis gas cooled.Thus, the gas treating re-heat of synthesis gas to be cooled and purification separation purified treatment is carried out heat exchange process, synthesis gas is cooled, without the need to external source, achieve reasonable, the efficiency utilization of energy.According to some embodiments of the present invention, the temperature of the first synthesis gas is-100 ~-140 DEG C.
According to embodiments of the invention, the method comprises further: before the first heat exchange process, carry out pretreatment to described synthesis gas, remove the impurity in described synthesis gas, so that the synthesis gas after being purified, this synthesis gas is applicable to ice chest process.Thus, by pretreatment, remove the impurity such as moisture content, carbon dioxide and the methyl alcohol in synthesis gas, and then, avoid above-mentioned medium and accumulate in ice chest, condense and occluding device or damage equipment.
According to embodiments of the invention, utilize heat exchanger package to carry out heat exchange cooling process to high pressure nitrogen, obtain liquid nitrogen, this liquid nitrogen is divided into three strands, and one cleaning solution as scrubber overhead 400 carries out washing to synthesis gas and refines; One stock-traders' know-how heat exchanger package enters synthesis gas pipeline, joins nitrogen to gas phase, and in gas phase, the volume ratio of nitrogen and hydrogen is (2.8 ~ 3.2): 1, preferably, is 3:1; One (on a small quantity) enters condenser 510 pairs of methane towers 500 and exports condensate liquid and cool, and produces phegma, increases the methane gas rate of recovery.Thus, utilize high pressure nitrogen to liquefy as low-temperature receiver, substantially provide low-temperature receiver without device outside, just can realize refining containing methane synthesis gas, reclaimed methane wherein to greatest extent simultaneously, obtained high-purity methane product.
S200 lowers the temperature process
According to embodiments of the invention, methane tower reboiler is utilized the first synthesis gas to be carried out cooling process.Obtain the second synthesis gas after lowering the temperature and heat, wherein, this heat is the heat supply of methane tower.Thus, utilize the first synthesis gas at the heat of cooling process release, be the heat supply of methane tower, achieve reasonable, the efficiency utilization of energy.According to some embodiments of the present invention, the temperature of described second synthesis gas is-110 ~-150 DEG C.
S300 second heat exchange process
According to embodiments of the invention, utilize heat exchanger package that the second synthesis gas is carried out the second heat exchange process, make the methane liquefaction in the second synthesis gas, obtain gas-liquid mixture.Thus, again utilize heat exchanger package to carry out heat exchange cooling process, utilize the condensing temperature of methane and other gas poor, make the methane liquefaction in the second synthesis gas.According to some embodiments of the present invention, the temperature of gas-liquid mixture is-170 ~-190 DEG C.
S400 separating treatment
According to embodiments of the invention, utilize gas-liquid separator that gas-liquid mixture is carried out separating treatment, to obtain gas phase and liquid phase.Thus, be separated from gas-liquid mixture and obtain liquid phase, this liquid phase is methane.
S500 carrying out washing treatment
According to embodiments of the invention, scrubbing tower is utilized to carry out carrying out washing treatment to described gas phase, so that the gas phase after being purified.Thus, the purity of gas phase is high.
According to some embodiments of the present invention, gas phase contains nitrogen and hydrogen, and hydrogen: the volume ratio of nitrogen is greater than 3:1.
According to some embodiments of the present invention, liquid nitrogen is utilized to carry out carrying out washing treatment.Thus, the purity of gas phase is high, and does not introduce impurity, and with the addition of nitrogen in gas phase, makes the volume ratio of nitrogen and hydrogen in gas phase close to 1:3.
S600 the 3rd heat exchange process
According to embodiments of the invention, utilize heat exchanger package to carry out the 3rd heat exchange process to the gas phase after purification, obtain the gas phase of re-heat.Thus, utilize the synthesis gas to be cooled of normal temperature to carry out re-heat by heat exchange to gas phase to gas phase, achieve reasonable, the efficiency utilization of energy.
According to some embodiments of the present invention, when utilizing heat exchanger package to carry out the 3rd heat exchange process to the gas phase after purification, the nitrogen of other passages in this heat exchanger package can be utilized to carry out distribution to this gas phase, make the volume ratio of nitrogen and hydrogen for (2.8 ~ 3.2): 1, preferably, be 3:1.
S700 first rectification process
According to embodiments of the invention, utilize methane tower to carry out the first rectification process to liquid phase, obtain the gas phase after the liquid phase after rectifying and rectifying.Thus, the purity of liquid and gas is higher, and then the purity of methane gas and fuel gas is higher.
S800 heating evaporation and the second rectification process
According to embodiments of the invention, methane reboiler is utilized the liquid phase after described rectifying to be carried out heating evaporation and the second rectification process, to obtain methane-rich liquid.Thus, be further purified liquid phase, in the methane-rich liquid obtained, methane content is higher.
According to some embodiments of the present invention, in methane-rich liquid, methane content is not less than 96%.
S900 the 4th heat exchange process
According to embodiments of the invention, utilize heat exchanger package that methane-rich liquid is carried out the 4th heat exchange process, to obtain methane gas, this methane gas is the methane gas of re-heat.Thus, utilize the synthesis gas to be cooled of normal temperature to carry out re-heat to methane-rich liquid by heat exchanger package, obtain the methane gas of normal temperature, achieve reasonable, the efficiency utilization of energy.
S1000 the 5th heat exchange process
According to embodiments of the invention, utilize described heat exchanger package that the gas phase after described rectifying is carried out the 5th heat exchange process, to obtain fuel gas, this fuel gas is the fuel gas of re-heat.Thus, utilize the synthesis gas to be cooled of normal temperature to carry out re-heat to gas phase by heat exchanger package, obtain the fuel gas of normal temperature, achieve reasonable, the efficiency utilization of energy.
According to some embodiments of the present invention, the gas phase after rectifying comprises nitrogen, methane, hydrogen and carbon monoxide.
According to the method for the embodiment of the present invention, provide low-temperature receiver without the need to outside, just can realize refining containing methane synthesis gas, reclaim methane wherein simultaneously to greatest extent, obtain high-purity methane product, and, the method simple to operate, investment and operating cost low, security is good, and treatment effeciency is high.
According to embodiments of the invention, the method comprises further: carry out pretreatment to described synthesis gas, removes the impurity in described synthesis gas, so that the synthesis gas after being purified, this synthesis gas is applicable to ice chest process.
According to embodiments of the invention, the temperature of described first synthesis gas is-100 ~-140 DEG C; The temperature of described second synthesis gas is-110 ~-150 DEG C; The temperature of described 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 illustrative, and can not be interpreted as limitation of the present invention.
Embodiment 1
The purification separation device of synthesis gas is utilized to carry out purification separation process to the synthesis gas of coal gasification, and utilize the hydrogen nitrogen ammonia synthesis being separated and obtaining, wherein, the component of the synthesis gas of this coal gasification is: hydrogen 78%, methane 19%, nitrogen 0.1%, carbon monoxide 2%, argon gas 0.1% and ethane 1%.Meanwhile, carry out refining to the synthesis gas of coal gasification by the method for deep cooling and scrubbing with liquid nitrogen and obtain high-purity methane product, wherein, as shown in Figure 1, the step utilizing this device to carry out purification separation process to synthesis gas is as follows for the structure of purification separation device:
(1) utilize pretreatment unit to carry out pretreatment to synthesis gas, remove the impurity such as moisture, carbon dioxide, methyl alcohol and the dust in synthesis gas, obtain the synthesis gas of dry applicable ice chest process.
(2) dry synthesis gas enters heat exchanger 110 channel B 3, and temperature is down to-110 ~-140 DEG C.Simultaneously, high pressure nitrogen (pressure is combined to atmospheric pressure higher than Import Gas) is successively by heat exchanger 120 passage A5, heat exchanger 110 channel B 6, temperature is down to-170 ~-190 DEG C, liquefaction of nitrogen is liquid nitrogen, wherein, fraction liquid nitrogen enters scrubbing tower 400 as scrubbing tower tower top cleaning solution, major part liquid nitrogen synthesis gas through heat exchanger 110 time allocate a certain amount of nitrogen into by channel B 8, become qualified hydrogen nitrogen synthesis gas to send, small part liquid nitrogen enters methane tower 500 as refrigerant and pushes up condenser 510, after providing cold to overhead condenser 510, through heat exchanger 110 channel B 1, after heat exchanger 120 passage A1 re-heat becomes normal temperature, enter air.
(3) synthesis gas that step (2) obtains enters methane tower reboiler 200, evaporation heat is provided to methane tower 500, self be cooled to-120 ~-150 DEG C, enter the channel B 7 of heat exchanger 110 subsequently, temperature is down to-170 ~-190 DEG C, now most in gasification synthesis gas methane liquefaction, obtains gas-liquid mixed media.
(4) gas-liquid mixed media enters knockout drum 300 centre entrance, the upper end outlet of knockout drum 300 is communicated with scrubbing tower 400 lower entrances, the isolated gas phase of knockout drum 300 enters scrubbing tower 400, obtains refining purified gas (H through scrubbing with liquid nitrogen
2: N
2volume ratio is greater than 3:1), fine gas through heat exchanger 110 channel B 5, heat exchanger 120 passage A4 re-heat be normal temperature, synthesis gas through heat exchanger 110 time, a certain amount of nitrogen is allocated into by channel B 8, become qualified hydrogen nitrogen synthesis gas (12) to send, wherein, H2:N2 volume ratio=3:1 in hydrogen nitrogen synthesis gas.
(5) the lower end outlet of knockout drum 300 is communicated with in the middle part of methane tower 500 through expenditure and pressure valve 700, liquid in knockout drum 300 is through throttling, enter methane tower 500, through heating evaporation and the rectifying separation of methane tower reboiler 200, the methane-rich liquid that purity is very high is obtained, CH4% > 96% in this methane-rich liquid bottom methane tower 500.
(6) bottom methane tower 500, liquid methane, after choke valve 700 reduces pressure throttling expansion, is sent outside as methane gas product after after heat exchanger 110 channel B 4, heat exchanger 120 passage A3 re-heat to normal temperature, in methane gas product, and methane+ethane >=98%.
(7) gas phase at methane tower 500 top is through overhead condenser 510 heat exchange, and partial gas phase liquefies, and flows back to methane tower 500 tower top as phegma.Methane tower 500 top fixed gas is sent outside as fuel gas after becoming normal temperature through heat exchanger 110 channel B 2, heat exchanger 120 passage A2 re-heat, and in this fuel gas component, methane content is less than 1%.
In the description of this description, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present invention or example.In this manual, identical embodiment or example are not necessarily referred to the schematic representation of above-mentioned term.And the specific features of description, structure, material or feature can combine in an appropriate manner in any one or more embodiment or example.
Although illustrate and describe embodiments of the invention, those having ordinary skill in the art will appreciate that: can carry out multiple change, amendment, replacement and modification to these embodiments when not departing from principle of the present invention and aim, scope of the present invention is by claim and equivalents thereof.
Claims (10)
1. a purification separation device for synthesis gas, described synthesis gas contains methane, it is characterized in that, comprising:
Heat exchanger package, for carrying out the first heat exchange process to described synthesis gas, to obtain the first synthesis gas cooled;
Methane tower reboiler, described methane tower reboiler is connected with described heat exchanger package, for described first synthesis gas being carried out cooling process, to obtain the second synthesis gas and heat;
Second synthesis gas return pipeline, described second synthesis gas return pipeline is connected with described methane tower reboiler with described heat exchanger package, for described second synthesis gas is delivered to described heat exchanger package, described heat exchanger package is utilized to carry out the second heat exchange process, to make the methane liquefaction in described second synthesis gas, obtain gas-liquid mixture;
Gas-liquid separator, described gas-liquid separator is connected with described heat exchanger package, for described gas-liquid mixture is carried out separating treatment, to obtain gas phase and liquid phase;
Scrubbing tower, described scrubbing tower is connected with described heat exchanger package with described gas-liquid separator, for carrying out carrying out washing treatment to described gas phase, so that the gas phase after being purified;
First gas phase pipeline, described first gas phase pipeline is connected with described heat exchanger package with described scrubbing tower, for by the extremely described heat exchanger package of the gas-phase transport after described purification, utilizes described heat exchanger package to carry out the 3rd heat exchange process, to obtain the gas phase of re-heat; Methane tower, described methane tower is connected with described heat exchanger package with described gas-liquid separator, described methane tower reboiler, described scrubbing tower, for carrying out the first rectification process to described liquid phase, to obtain the gas phase after the liquid phase after rectifying and rectifying;
Liquid phase pipeline, described liquid phase pipeline is connected with described methane tower reboiler with described methane tower, for the liquid phase after described rectifying being delivered to described methane tower reboiler, described heat is utilized to carry out heating evaporation and the second rectification process, to obtain methane-rich liquid, more described methane-rich liquid is returned described methane tower;
Methane-rich liquid pipeline, described methane-rich liquid pipeline is connected with described heat exchanger package with described methane tower, for described methane-rich liquid is delivered to described heat exchanger package, utilizes described heat exchanger package to carry out the 4th heat exchange process, to obtain methane gas; And
Second gas phase pipeline, described second gas phase pipeline is connected with described heat exchanger package with described methane tower, for by the extremely described heat exchanger package of the gas-phase transport after described rectifying, utilizes described heat exchanger package to carry out the 5th heat exchange process, to obtain fuel gas.
2. device according to claim 1, is characterized in that, comprises further:
Pretreatment unit, for carrying out pretreatment to described synthesis gas, removes the impurity in described synthesis gas, so that the synthesis gas after being purified.
3. device according to claim 1, is characterized in that, described heat exchanger package comprises First Heat Exchanger and the second heat exchanger,
Optionally, First Heat Exchanger and the second heat exchanger are plate-fin heat exchanger.
4. device according to claim 1, is characterized in that, described scrubbing tower and methane tower are plate column or packed tower,
Optionally, described methane tower reboiler is built-in thermosiphon reboiler or external thermosiphon reboiler.
5. device according to claim 1, is characterized in that, described methane tower comprises further:
Condenser, described condenser is arranged on the top of described methane tower, for carrying out condensation process to the gas phase after described rectifying, makes the methane condensation liquefaction in the gas phase after described rectifying, and backflow mixes with described methane-rich liquid.
6. device according to claim 1, is characterized in that, described gas-liquid separator is connected by expenditure and pressure valve with described methane tower.
7. utilize a method for the device purification separation synthesis gas described in any one of claim 1 ~ 6, described synthesis gas contains methane, it is characterized in that, comprising:
Heat exchanger package is utilized to carry out the first heat exchange process to described synthesis gas, to obtain the first synthesis gas cooled;
Utilize methane tower reboiler described first synthesis gas to be carried out cooling process, to obtain the second synthesis gas after lowering the temperature and heat, wherein, described heat is the heat supply of methane tower;
Utilize heat exchanger package that described second synthesis gas is carried out the second heat exchange process, make the methane liquefaction in described second synthesis gas, to obtain gas-liquid mixture;
Utilize gas-liquid separator that described gas-liquid mixture is carried out separating treatment, to obtain gas phase and liquid phase;
Scrubbing tower is utilized to carry out carrying out washing treatment to described gas phase, so that the gas phase after being purified;
Described heat exchanger package is utilized to carry out the 3rd heat exchange process to the gas phase after described purification, to obtain the gas phase of re-heat;
Methane tower is utilized to carry out the first rectification process to described liquid phase, to obtain the gas phase after the liquid phase after rectifying and rectifying;
Methane reboiler is utilized the liquid phase after described rectifying to be carried out heating evaporation and the second rectification process, to obtain methane-rich liquid;
Utilize described heat exchanger package that described methane-rich liquid is carried out the 4th heat exchange process, to obtain described methane gas; And
Described heat exchanger package is utilized the gas phase after described rectifying to be carried out the 5th heat exchange process, to obtain fuel gas.
8. method according to claim 7, is characterized in that, comprises further
Described heat exchanger package is utilized to carry out described 6th heat exchange process, to obtain liquid nitrogen to high pressure nitrogen;
A part for described liquid nitrogen is utilized to carry out described carrying out washing treatment, so that the gas phase after being purified;
A part for described liquid nitrogen is added in described gas phase, to obtain joining nitrogen phase, wherein, described in join nitrogen mutually in the volume ratio of hydrogen and nitrogen be (2.8 ~ 3.2): 1, preferably, be 3:1; And
Utilize a part for described liquid nitrogen to carry out condensation process to the gas phase after described rectifying, to make the methane condensation liquefaction in the gas phase after described rectifying, and backflow mixes with described methane-rich liquid,
Optionally, the partially liq at the bottom of described scrubbing tower tower is back in described methane tower, and mixes with described methane-rich liquid.
9. method according to claim 7, is characterized in that, comprises further:
Pretreatment is carried out to described synthesis gas, removes the impurity in described synthesis gas, so that the synthesis gas after being purified.
10. method according to claim 7, is characterized in that,
The temperature of described first synthesis gas is-100 ~-140 DEG C;
The temperature of described second synthesis gas is-110 ~-150 DEG C;
The temperature of described gas-liquid mixture is-170 ~-190 DEG C.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105861086A (en) * | 2016-05-10 | 2016-08-17 | 中国科学院理化技术研究所 | Technique of utilizing gasified coal gas and coke oven gas to co-produce liquefied natural gas, methanol and liquid ammonia |
| 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 |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
-
2015
- 2015-08-20 CN CN201510514031.3A patent/CN105066585B/en active Active
Patent Citations (5)
| 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 |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105861086A (en) * | 2016-05-10 | 2016-08-17 | 中国科学院理化技术研究所 | Technique of utilizing gasified coal gas and coke oven gas to co-produce liquefied natural gas, methanol and liquid ammonia |
| CN105861086B (en) * | 2016-05-10 | 2019-04-26 | 中国科学院理化技术研究所 | Utilize the process of gasification gas and coke-stove gas co-production of liquefied natural gas, methanol and liquefied ammonia |
| 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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