CN210419229U - Conversion system for preparing methanol by gasifying coal water slurry - Google Patents
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- CN210419229U CN210419229U CN201921429793.3U CN201921429793U CN210419229U CN 210419229 U CN210419229 U CN 210419229U CN 201921429793 U CN201921429793 U CN 201921429793U CN 210419229 U CN210419229 U CN 210419229U
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Abstract
The utility model belongs to the technical field of coal chemical industry, and relates to a conversion system for preparing methanol by gasifying coal water slurry, which comprises a separator, a conversion furnace, a steam superheater and a waste boiler; the inlet of the separator is connected with the crude gas; the top outlet of the separator is respectively connected with the shell pass inlet of the shift converter and the tube pass inlet of the waste boiler; a tube pass outlet of the shift converter is connected to a superheated steam pipe network; two outlet pipelines are arranged at a shell pass outlet of the shift converter, and one outlet pipeline is connected with a shell pass inlet of the steam superheater; the tube side inlet of the steam superheater is connected with the shell side outlet of the waste boiler; the shell side inlet of the waste boiler is connected with a boiler water pipe; the conversion system for preparing the methanol by gasifying the coal water slurry also comprises a steam pipeline; the steam pipeline is respectively connected with a tube side inlet of the shift converter and a tube side inlet of the steam superheater. The utility model discloses the system operation is stable, and the transform is effectual, and catalyst life cycle extension, high-order heat can high-efficient quantization, rational utilization.
Description
Technical Field
The utility model belongs to the technical field of the coal industry, a methyl alcohol transform system is related to, in particular to coal slurry gasification system methyl alcohol transform system.
Background
The conversion process is an important process in the coal chemical industry and is used for converting excessive CO into H2The transformation process mainly comprises the following steps according to different gasification processes: the normal pressure gas making is matched with the conversion, the step-by-step intermediate cooling and the humidification are carried out, and the stable operation of the conversion is controlled. In the process of preparing methanol by gasifying coal water slurry, when the steam gas of raw coal gas is high and the gas pressure is high, the existing conversion process has the following problems: most of the shift converters are subjected to axial adiabatic or axial radial adiabatic shift, the utilization of high-level heat is poor, the high-level heat of steam produced by system synthesis is mostly used for superheating steam without producing steam, and meanwhile, a non-shift byproduct is part of steam; the temperature of a catalyst bed layer in the shift reactor is high and is difficult to control, the shift reaction driving force is large, the service cycle of the catalyst is 2-4 years, the service life is short, and the shift reaction efficiency is influenced.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem that high-order heat utilization is unreasonable, catalyst activity is low, the life-span is short among the background art, the utility model provides an operation is stable, high-order heat energy high efficiency quantization, rational utilization for change bed layer temperature can effective control, and catalyst activity is good, and transform effect is good, and the coal slurry gasification system methanol conversion system that catalyst life cycle can prolong.
In order to realize the purpose, the technical scheme of the utility model is that:
a coal water slurry gasification system methanol shift system which characterized in that: the conversion system for preparing the methanol by gasifying the coal water slurry comprises a separator, a conversion furnace, a steam superheater and a waste boiler;
the separator is provided with an inlet, a top outlet and a bottom outlet; the shift converter, the steam superheater and the waste boiler are respectively provided with a tube pass inlet, a shell pass inlet, a tube pass outlet and a shell pass outlet;
the top outlet of the separator is respectively connected with the shell pass inlet of the shift converter and the tube pass inlet of the waste boiler; the tube pass outlet of the shift converter is connected to a superheated steam pipe network; two outlet pipelines are arranged at a shell pass outlet of the shift converter, and one outlet pipeline is connected with a shell pass inlet of the steam superheater; the tube side inlet of the steam superheater is connected with the shell side outlet of the waste boiler; the shell side inlet of the waste boiler is connected with a boiler water pipe.
Further, the coal water slurry gasification methanol preparation conversion system also comprises a steam pipeline; and the steam pipeline is respectively connected with a tube side inlet of the shift converter and a tube side inlet of the steam superheater.
Further, the coal water slurry gasification methanol preparation conversion system also comprises a first heat exchanger and a second heat exchanger; an outlet at the top of the separator is connected with a shell pass inlet of the shift converter through a first heat exchanger; the steam pipeline is connected with a tube pass inlet of the shift converter through a second heat exchanger; and the shell pass outlet pipeline of the shift converter passes through a second heat exchanger.
Further limiting, the shift converter is a spiral tube heat exchange type shift converter; a catalyst bed layer is arranged in the shell side of the shift converter; the catalyst bed layer is arranged into an upper layer and a lower layer.
Further defined, the catalyst bed is a sulfur tolerant shift catalyst bed.
A conversion method based on a conversion system for preparing methanol by gasifying coal water slurry is characterized in that: the transformation method comprises the following steps:
1) the raw gas gasified by the water-coal-slurry enters a separator from the inlet of the separator, is divided into two paths after being separated by the water-gas, and one path is that part of the raw gas after being separated by the water-gas enters the tube pass of a waste boiler and then is sent to a system for preparing methanol after conversion; one path is that part of the crude gas after water gas separation enters the step 2);
2) the crude gas after part of water gas is separated enters a shell pass of a shift converter through a first heat exchanger, and is subjected to shift reaction under the action of a catalyst bed layer; meanwhile, saturated steam enters a tube pass of the shift converter from the steam pipeline through a second heat exchanger, and heat in a shell pass of the shift converter is transferred to control the temperature of a shift reaction in the shell pass of the shift converter; after the raw gas transformed by the shift converter flows out from a shell pass outlet of the shift converter, part of the transformed raw gas is subjected to heat exchange by a second heat exchanger and then is sent into a transformed system to prepare methanol; part of the transformed raw gas enters the step 3);
3) part of the transformed crude gas enters the shell side of the steam superheater; saturated steam from the outer pipe enters the tube pass of the steam superheater through a steam pipeline, and superheated boiler water from the waste boiler shell pass enters the tube pass of the steam superheater; the converted crude gas in the middle part of the shell pass of the steam superheater and saturated steam in the tube pass of the steam superheater are subjected to superheat exchange, and then methanol is prepared from a shell pass outlet at the bottom of the steam superheater to a converted system; and the superheated steam at the outlet of the steam superheater tube pass is sent to a system steam pipe network.
Further limiting, the crude gas gasified by the coal water slurry is a mixed gas of steam and dry gas; the dry gas comprises CO and H2、CO2And residual gas; the residual gas is N2、CH4And H2And (4) S gas.
Further limiting, the volume ratio of steam to dry gas in the crude gas gasified by the coal water slurry is 1.0-1.4; the dry gas comprises 35-45% of CO and 38-44H2、15-20％CO21-2% of residual gas; the pressure of the crude gas gasified by the coal water slurry is 4-6.5 MPa.
Further limiting, the volume ratio of steam to dry gas in the crude gas is 1.2; the dry gas comprises 40% of CO and 40% of H2、18.5％CO2And 1.5% residual gas; the pressure of the crude gas is 6.2 MPa.
Further, the saturated steam is 2.5MPa saturated steam.
The utility model has the advantages that:
1. the utility model provides a conversion system and a conversion method for preparing methanol by gasifying coal water slurry, wherein, the raw coal gas is divided into two branches after separation, one branch is connected with a shell pass inlet of a conversion furnace, and the other branch is sent into a conversion system through a tube pass of a waste boiler; the tube pass inlet of the shift converter is connected with saturated steam from the outer tube; a tube pass outlet of the shift converter is connected to a superheated steam pipe network; the shell pass outlet of the shift converter comprises two branches, one branch is sent into a post-shift system after being subjected to shell pass overheating through a steam superheater, the other branch is sent into the post-shift system after being subjected to heat exchange, and a tube pass inlet of the steam superheater is simultaneously connected with saturated steam from an outer tube and a shell pass outlet of a waste boiler; the shell side inlet of the waste boiler is connected with boiler water. The utility model discloses under higher vapour-gas ratio, the temperature of catalyst bed is in lower scope, and CO content is low in the process gas after the transform, and transform effectually, and transform the H in the back gas2The volume ratio of the catalyst to CO meets the requirement of methanol preparation, and meanwhile, the high-level heat of the system can be reasonably utilized, and the process operation of the system is stable.
2. The utility model discloses a shift converter is spiral pipe heat transfer formula shift converter, is provided with the catalyst bed in the shift converter shell side, and the catalyst bed sets up to upper and lower two-layer. The catalyst bed in the shift converter has small resistance, low production capacity, long service life and low production cost.
Drawings
FIG. 1 is a process flow diagram of a shift system for producing methanol by gasifying coal water slurry;
wherein:
1-a separator; 2-waste pot; 3-steam superheater; 4-a shift converter; 5-a first heat exchanger; 6-second heat exchanger.
Detailed Description
The present invention will now be described in detail with reference to the accompanying drawings and examples.
Example 1
Referring to fig. 1, the utility model provides a coal slurry gasification system methyl alcohol transform system and transform method includes separator 1, shift converter 4, steam superheater 3, waste boiler 2, first heat exchanger 5 and second heat exchanger 6.
In the utility model, the inlet of the separator 1 is connected with the raw gas from gasification; the bottom outlet of the separator 1 is connected to a system pipe network; the top outlet of the separator 1 comprises two branches, and one branch is connected with the shell pass inlet of the shift converter 4 through a first heat exchanger 5; the other branch is connected with a tube pass inlet of the waste pot 2 and is sent to a system for preparing methanol after conversion through the tube pass of the waste pot 2; a tube pass inlet of the shift converter 4 is connected with a steam pipeline, and saturated steam from the outer tube flows into the steam pipeline and is connected with the tube pass inlet of the shift converter 4 through a second heat exchanger 6; a tube pass outlet of the shift converter 4 is connected to a superheated steam pipe network; the shell pass outlet of the shift converter 4 comprises two branches, one branch is connected with the shell pass inlet of the steam superheater 3, and the other branch enters the shell pass inlet of the shift converter 4 again after passing through the second heat exchanger 6; a shell pass outlet of the steam superheater 3 is communicated with a system after conversion, and the system after conversion is a methanol preparation system; a tube side inlet of the steam superheater 3 is simultaneously connected with a steam pipeline and a shell side outlet of the waste boiler 2; the shell pass inlet of the waste boiler 2 is connected with boiler water; the utility model provides a shift converter 4 is spiral pipe heat transfer formula shift converter, and 4 shell sides of shift converter are filled with the catalyst bed, and the catalyst bed sets up for two layers from top to bottom, and during the implementation, the catalyst is sulfur-tolerant shift catalyst, and for example the catalyst is cobalt molybdenum sulfur-tolerant shift catalyst; the structure of the steam superheater 3 is a spiral pipe type.
The raw gas adopted in the utility model is the mixed gas of steam and dry gas; the dry gas comprises CO and H2、CO2And the residual gas is N2、CH4And H2S gas; the volume ratio of steam to dry gas in the raw gas is 1.0-1.4; the pressure of the crude gas is 4.0-6.5 MPa; the dry gas has 35-45% of CO and 38-42% of H215-20% of CO2 and 1-2% of residual gas. Preferably, the volume ratio of steam to dry gas in the raw gas is 1.2; the pressure of the crude gas is 6.2 MPa; the dry gas comprises 40% of CO and 40% of H2、18.5％CO2And 1.5% residual gas. Saturated steam from the outer tube is 25MPa saturated steam. The utility model provides a transform system mainly is applicable to the transform of CO in the raw gas of high vapour-gas ratio, higher pressure, and transform efficiency is high, and the thermal efficiency is utilized well.
Example 2
According to the process diagram of embodiment 1, the transformation flow of the specific transformation system of the present invention is: after the gasified crude gas is subjected to water gas separation in the separator 1, the waste liquid is discharged to a system pipe network from a bottom outlet of the separator 1; the separated process gas is discharged from a top outlet of the separator 1 and is divided into two branches, wherein one branch is a top shell pass inlet of a shift converter 4 after part of the process gas passes through a first heat exchanger 5, and generates CO shift reaction under the action of a catalyst in the shell pass of the shift converter 4, and the other branch is a system after part of the process gas enters a tube pass inlet of a waste pot 2 and is subjected to heat exchange by the waste pot 2; in the shift converter 4, 2.5MPa saturated steam from an outer pipe enters a pipe pass inlet at the top of the shift converter 4 after heat exchange is carried out on the saturated steam through a steam pipe by a second heat exchanger 6, so that the temperature of the saturated steam entering the shift converter 4 is increased, and the dew point at the inlet of the shift converter 4 is prevented; 2.5MPa saturated steam in the tube pass of the shift converter 4 exchanges heat with reaction gas in the shell pass of the shift converter 4, so that heat emitted by the shift reaction of the shell pass of the shift converter 4 is transferred away, the temperature of the shift reaction is kept in a certain range, and the shift reaction is accelerated; after a large amount of heat is exchanged in the tube pass of the shift converter 4 by the saturated steam with the pressure of 2.5MPa, discharging the superheated steam with the pressure of 2.5MPa from an outlet of the tube pass at the bottom of the shift converter 4 to a superheated steam pipe network; the process gas is subjected to shift reaction on the shell side of the shift converter 4, then comes out from a shell side outlet at the bottom of the shift converter 4 and is divided into two branch circuits, wherein one branch circuit is formed by leading part of the shifted process gas to enter the steam superheater 3 from a shell side inlet at the top of the steam superheater 3, performing heat exchange with steam in a tube side of the steam superheater 3, and then leading the steam to be transmitted to a post-shift system from a shell side outlet at the bottom of the steam superheater 3, the steam in the tube side of the steam superheater 3 is steam from a shell side outlet of the waste boiler 2 and 2.5MPa saturated steam from the outside of the tube, and the heat of the part of the shifted process gas in the shell side of the steam superheater 3 can be transferred and discharged to a superheated steam pipe network from a tube side outlet; the other branch part enters a second heat exchanger 6 for heat exchange through the transformed process gas and then is sent to a methanol preparation system.
Example 3
The utility model discloses a transform furnace 4 be spiral pipe heat transfer formula transform furnace, steam over heater 3's structure be the spiral tube formula, transform furnace 4 and steam over heater 3 are axial formula reaction tower, and the reaction equipment structure is simple relatively, reliable.
The shift converter 4 is filled with a catalyst bed layer in the shell side, the catalyst bed layer is divided into an upper layer and a lower layer, and the catalyst is a sulfur-tolerant shift cobalt-molybdenum catalyst, such as a common DQB04 or DQB204 catalyst on the market. The operation temperature of the catalyst is low, and is generally 230-330 ℃; the carbon monoxide is lower after the conversion; has strong sulfur toxicity resistance.
Example 4
The raw gas obtained after the coal water slurry gasification is taken as an example to illustrate the conversion system and the conversion method for preparing the methanol by the coal water slurry gasification provided by the utility model, the raw gas comes from the gasification, the pressure is 6.2MPa, the temperature is 240 ℃, the volume ratio of steam to dry gas is 1.2, wherein the dry gas contains 40 percent of CO and 40 percent of H respectively2、18.5％CO2And 1.5% residual gas.
After the crude gas is subjected to coal-water separation by the separator, the separated liquid and the like are discharged to a system pipe network from an outlet at the bottom of the separator 1; the separated process gas is carried out of the separator from the top outlet of the separator 1, and the process gas is divided into two branches:
one of the two exchanges heat by the first heat exchanger 5, the crude gas with the temperature of 260 ℃ enters a shift converter and undergoes a shift reaction of CO + H under the action of a catalyst2O＝CO2+H2+ Q, the shift converter 4 is a spiral tube heat exchange type shift converter, the shell side of the shift converter is filled with DQB04 catalyst in two layers, saturated steam with about 2.5MPa flows from top to bottom in the tube side of the shift converter 4, the preheated raw gas exchanges heat with the catalyst layer outside the shift converter 4 to raise the temperature, one part of the heat generated by the reaction of the catalyst layer is transferred to the steam in the shift converter 4 tube through heat exchange, the other part of the heat is carried out of the shift converter along with the process gas, the process gas out of the shift converter 4 is divided into two branches, one branch is the process gas out of the shift converter 4 and passes through the steam superheater3, the superheated process gas enters a system after conversion, and the process gas of the other furnace 4 enters the system after conversion after heat exchange by the second heat exchanger 6. In the implementation, in the shift converter 4, the CO content in the process gas after the shift converter is 3 percent and the H content is 3 percent under the condition of DQB04 catalyst and the temperature of 265 DEG C2The volume ratio of the gas to CO is 2.1, the requirement of preparing the methanol is met, and the converted process gas is sent to a converted methanol preparing system after heat exchange.
The other separated crude gas enters a tube pass of the waste boiler 2 and exchanges heat with boiler water entering a shell pass of the waste boiler 2, and then the crude gas is sent to a system after conversion from a tube pass outlet of the waste boiler 2; boiler water comes out from a shell side outlet of the waste boiler 2 and is mixed with saturated steam of 2.5MPa, and then the mixture enters a tube side inlet at the top of the steam superheater 3 to exchange heat with gas in a tube side of the steam superheater 3.
Therefore, the utility model discloses the heat that produces in the shift converter, a part and 4 intraductal from top to bottom of shift converter walk about 2.5 MPa's saturated steam and carry out the heat transfer, another part heat goes out shift converter 4 along with process gas, and the process gas that goes out shift converter 4 divides into two branches, and one branch is overheated through steam superheater 3, and another shift converter process gas gets into shift converter 4 again after preheating through second heat exchanger 6 and carries out the shift reaction; the system has high heat utilization rate, reasonable high-level heat utilization, stable operation and high conversion efficiency.
In the conversion reaction process, the temperature of the catalyst bed layer in the shell pass of the conversion furnace 4 is 300 ℃, the temperature of the catalyst bed layer is low, the continuous conversion reaction is favorably carried out, meanwhile, the damage of the bed layer temperature to the catalyst is small, the service cycle of the catalyst can be prolonged, and the operation cost is saved.
Example 5
The difference from example 4 is: the pressure of the raw gas from gasification is 4.0MPa, and the volume ratio of steam to dry gas is 1.4, wherein the dry gas contains 45% of CO and 38% of H respectively2、15％CO2And 2% residual gas.
The separated raw gas enters a shift converter 4, the shift of CO can be realized by the shift system under the condition of DQB04 catalyst and the temperature of 230 ℃, the CO content in the process gas passing through the shift converter is 3.5 percent, and H is H2The volume ratio of the catalyst to CO is 2.15, the requirement of methanol preparation is met, the converted process gas is superheated by the steam superheater and then is sent into a converted methanol preparation system, the heat of the whole system can be reasonably utilized, the activity of the catalyst is good, and the system is stable in operation.
Example 6
The difference from example 4 is: the pressure of the raw gas from gasification is 5.0MPa, and the volume ratio of steam to dry gas is 1.0, wherein the dry gas contains 38% of CO and 38% of H respectively2、18％CO2And 2% residual gas.
The raw gas enters a shift converter 4 after being separated, the CO content in the process gas passing through the shift converter is 4 percent and the H content is H under the condition of DQB204 catalyst and the temperature is 330 DEG C2The volume ratio of the catalyst to CO is 2.06, the requirement of methanol preparation is met, the converted process gas is superheated by the steam superheater and then is sent into a converted methanol preparation system, the heat of the whole conversion system can be reasonably utilized, the activity of the catalyst is good, and the system is stable in operation.
Example 7
The difference from example 4 is: the pressure of the raw gas from gasification is 6.8MPa, and the volume ratio of steam to dry gas is 1.2, wherein the dry gas contains 35% of CO and 44% of H respectively2、20％CO2And 1% residual gas.
The raw gas enters a shift converter 4 after being separated, the CO content in the process gas passing through the shift converter 4 is 3 percent and H is carried out at the temperature of 280 ℃ under the condition of DQB204 catalyst2The volume ratio of the gas to CO is 2.15, the requirement of methanol preparation is met, and the converted process gas is superheated by a steam superheater and then is sent to a converted methanol preparation system.
According to the embodiment, the conversion system is suitable for the CO conversion process of the high-pressure and high-steam-gas-ratio crude gas, H2The volume ratio of the catalyst to CO meets the process requirement of preparing methanol, the system runs stably, the generated high-level heat is well utilized, the heat utilization efficiency is high, the temperature of a catalyst bed layer is low, and the service cycle of the catalyst is prolonged.
Claims (5)
1. A coal water slurry gasification system methanol shift system which characterized in that: the conversion system for preparing the methanol by gasifying the coal water slurry comprises a separator (1), a conversion furnace (4), a steam superheater (3) and a waste boiler (2);
the separator (1) is provided with an inlet, a top outlet and a bottom outlet; the shift converter (4), the steam superheater (3) and the waste boiler (2) are respectively provided with a tube pass inlet, a shell pass inlet, a tube pass outlet and a shell pass outlet;
the top outlet of the separator (1) is respectively connected with the shell-side inlet of the shift converter (4) and the tube-side inlet of the waste boiler (2); the tube pass outlet of the shift converter (4) is connected to a superheated steam pipe network; two outlet pipelines are arranged at a shell pass outlet of the shift converter (4), and one outlet pipeline is connected with a shell pass inlet of the steam superheater (3); a tube side inlet of the steam superheater (3) is connected with a shell side outlet of the waste boiler (2); the shell side inlet of the waste boiler (2) is connected with a boiler water pipe.
2. The shift system for producing methanol by gasifying coal-water slurry according to claim 1, wherein: the conversion system for preparing the methanol by gasifying the coal water slurry also comprises a steam pipeline; and the steam pipeline is respectively connected with a tube pass inlet of the shift converter (4) and a tube pass inlet of the steam superheater (3).
3. The shift system for producing methanol by gasifying coal-water slurry according to claim 2, wherein: the conversion system for preparing the methanol by gasifying the coal water slurry also comprises a first heat exchanger (5) and a second heat exchanger (6); an outlet at the top of the separator (1) is connected with a shell pass inlet of the shift converter (4) through a first heat exchanger (5); the steam pipeline is connected with a tube pass inlet of the shift converter (4) through a second heat exchanger (6); and a shell pass outlet pipeline of the shift converter (4) passes through a second heat exchanger (6).
4. The shift system for producing methanol by gasifying coal-water slurry according to claim 3, wherein: the shift converter (4) is a spiral tube heat exchange type shift converter; a catalyst bed layer is arranged in the shell side of the shift converter (4); the catalyst bed layer is arranged into an upper layer and a lower layer.
5. The shift system for producing methanol by gasifying coal-water slurry according to claim 4, wherein: the catalyst bed layer is a sulfur-tolerant shift catalyst bed layer.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110407169A (en) * | 2019-08-29 | 2019-11-05 | 陕西聚能新创煤化科技有限公司 | Coal water slurry gasification methanol transformation system and transform method |
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| CN110407169A (en) * | 2019-08-29 | 2019-11-05 | 陕西聚能新创煤化科技有限公司 | Coal water slurry gasification methanol transformation system and transform method |
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