CN104199413B - The urgent interlock shutdown method of coal-water slurry gasification system - Google Patents
The urgent interlock shutdown method of coal-water slurry gasification system Download PDFInfo
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- CN104199413B CN104199413B CN201410438966.3A CN201410438966A CN104199413B CN 104199413 B CN104199413 B CN 104199413B CN 201410438966 A CN201410438966 A CN 201410438966A CN 104199413 B CN104199413 B CN 104199413B
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- 238000002309 gasification Methods 0.000 title claims abstract description 112
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- 239000002002 slurry Substances 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 50
- 239000007789 gas Substances 0.000 claims abstract description 247
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- 238000003786 synthesis reaction Methods 0.000 claims abstract description 182
- 239000003245 coal Substances 0.000 claims abstract description 139
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 100
- 239000001301 oxygen Substances 0.000 claims abstract description 100
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 100
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- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910001882 dioxygen Inorganic materials 0.000 claims abstract description 11
- 238000001816 cooling Methods 0.000 claims description 108
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- 230000008569 process Effects 0.000 claims description 21
- 238000011084 recovery Methods 0.000 claims description 14
- 239000002826 coolant Substances 0.000 claims description 13
- 230000008676 import Effects 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 116
- 229910052757 nitrogen Inorganic materials 0.000 description 58
- 239000002956 ash Substances 0.000 description 46
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P90/00—Enabling technologies with a potential contribution to greenhouse gas [GHG] emissions mitigation
- Y02P90/02—Total factory control, e.g. smart factories, flexible manufacturing systems [FMS] or integrated manufacturing systems [IMS]
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Abstract
The invention provides a kind of urgent interlock shutdown method of coal-water slurry gasification system.This method includes：When the absolute value of the rate of temperature change of the absolute value of the rate of temperature change of absolute value, the oxygen channel being connected with coal gasifier when the rate of temperature change of coal gasifier and the synthesis gas flowed out from scrubbing tower is above the first preset value；And/or when the absolute value of the absolute value of pressure change rate of coal gasifier, the absolute value of the pressure change rate of oxygen channel and pressure change rate from the synthesis gas of scrubbing tower outflow is above the second preset value；And/or when abnormal conditions occur for compressor；And/or in oxygen channel, when abnormal conditions occur for the oxygen gas flow rate in the oxygen pipeline of center, make coal-water slurry gasification system shutdown.In accordance with the invention it is possible to carry out emergency shut-down control device to coal-water slurry gasification system exactly, ensure the operation stability and security of coal-water slurry gasification system, avoid the generation of accident.
Description
Technical field
The present invention relates to coal-water slurry gasification technical field, more particularly, to a kind of coal-water slurry gasification system
Urgent interlock shutdown method.
Background technology
In normal production, the coal-water slurry gasification system most of the time is in the running status of HTHP, and its
Internal work medium is also and its material of inflammable, explosive, poisonous property, it may be said that safety in production and safe operation are for water-coal-slurry
Gasification process system is extremely important, and gasification furnace security system is exactly to ensure the gasified boiler system safety connection safe for operation set up
Lock system, interlocking of especially stopping in emergency, it is even more safe important leverage.
In addition, in actual Chemical Manufacture, the situation of abnormal damage occurs in instrument sensing element, at this moment instrument transmission
Data often understand distortion, even result in the interlock shutdown of mistake, cause unnecessary loss.Usually by instrument in traditional method
The variate-value that sensing element senses go out simply carries out 3 and selects 2 computing then to judge whether interlock shutdown, when instrument sensing element
When abnormal distortion occurs, unnecessary interlock shutdown is easily caused, causes unnecessary economic loss.
It can be seen that the interlocking of stopping in emergency in existing Coal Gasification Technology is perfect not enough, it is impossible to ensures coal water slurry gasification
The safety movement of process system.
The content of the invention
The present invention is intended to provide a kind of urgent interlock shutdown method of coal-water slurry gasification system, to solve prior art
In the urgent interlock shutdown method of coal-water slurry gasification system cannot be guaranteed to meet coal-water slurry gasification system safety
The problem of operation.
A kind of in order to solve the above technical problems, according to an aspect of the invention, there is provided coal-water slurry gasification system
Urgent interlock shutdown method, the urgent interlock shutdown method of the coal-water slurry gasification system includes：When the temperature of coal gasifier
Spend the absolute value of rate of change, the oxygen channel being connected with coal gasifier rate of temperature change absolute value and from scrubbing tower outflow
The absolute value of rate of temperature change of synthesis gas when being above the first preset value, make coal-water slurry gasification system shutdown；And/or
The absolute value of the pressure change rate of absolute value, oxygen channel when the pressure change rate of coal gasifier and from scrubbing tower outflow
When the absolute value of the pressure change rate of synthesis gas is above the second preset value, make coal-water slurry gasification system shutdown；And/or work as
When abnormal conditions occur for compressor, make coal-water slurry gasification system shutdown；And/or in oxygen channel, when center oxygen hose
When abnormal conditions occur for the oxygen gas flow rate in road, make coal-water slurry gasification system shutdown.
Further, when the temperature of coal gasifier is higher than the 4th preset value higher than the temperature of the 3rd preset value or oxygen channel
Or from the temperature of synthesis gas of scrubbing tower outflow be higher than five preset values when, make coal-water slurry gasification system shutdown.
Further, the first preset value is within the scope of 0.4 DEG C/ms to 0.6 DEG C/ms.
Further, when the pressure of coal gasifier is higher than the 7th preset value higher than the pressure of the 6th preset value, oxygen channel
And from the pressure of synthesis gas of scrubbing tower outflow be higher than eight preset values when, make coal-water slurry gasification system shutdown.
Further, the abnormal conditions of compressor include：The outlet pressure of compressor is more than the 9th preset value；And/or pressure
The absolute value of pressure difference between the outlet of contracting machine and coal gasifier is higher than the tenth preset value or less than the 11st preset value；And/or
The absolute value of the pressure change rate of compressor is more than the 12nd preset value.
Further, abnormal conditions, which occur, for the oxygen gas flow rate in the oxygen channel of center includes：Oxygen stream in oxygen channel
Speed is more than the 13rd preset value.
Further, the second preset value is in the range of 9kpa/ms to 11kpa/ms.
Further, the 12nd preset value is in the range of 1.8kpa/ms to 2.2kpa/ms.
The technical scheme of application invention, the urgent interlock shutdown method combination coal water slurry gasification of coal-water slurry gasification system
In process system easily there is accident or the position for accident occur must be prevented, i.e., coal gasifier, oxygen channel, compressor with
And from scrubbing tower, combination temperature rate of change, pressure change rate and there is the conditions of abnormal conditions to realize coal water slurry gasification work
The condition of the urgent interlock shutdown of process system, emergency shut-down control device can be carried out to coal-water slurry gasification system exactly, protected
The operation stability and security of coal-water slurry gasification system are demonstrate,proved, avoids the generation of accident, essence can be carried out to whole system
True control, ensure the personal safety of operating personnel.During real work, if coal-water slurry gasification system meet it is any of the above described
One condition, the control centre of coal-water slurry gasification system perform shut-down operation with regard to control system.
Brief description of the drawings
The accompanying drawing for forming the part of the application is used for providing a further understanding of the present invention, schematic reality of the invention
Apply example and its illustrate to be used to explain the present invention, do not form inappropriate limitation of the present invention.In the accompanying drawings：
Fig. 1 diagrammatically illustrates the front view of the coal-water slurry gasification system in the present invention；
Fig. 2 diagrammatically illustrates the front view of the coal gasifier in the present invention；
The heat exchanger that Fig. 3 diagrammatically illustrates the present invention removes the top view after part enclosure；
Left view when Fig. 4 diagrammatically illustrates the doctor assemblies of the heat exchanger of the present invention on main shaft；
Fig. 5 diagrammatically illustrates the front view of the heat exchange unit of the heat exchanger of the present invention；
Fig. 6 diagrammatically illustrates the front view of the cooling device in the present invention；
Fig. 7 diagrammatically illustrates the front view of the first or second cyclone dust collectors of the present invention；
Fig. 8 diagrammatically illustrates Fig. 7 A-A views；
Fig. 9 diagrammatically illustrates the three-dimensional structure diagram of the guide in the present invention；
Figure 10 diagrammatically illustrates the front view of the scrubbing tower of the present invention；And
Figure 11 diagrammatically illustrates the annexation figure of the coal gasifier feed system of the present invention.
Description of reference numerals：10th, gasification unit；11st, coal gasifier；111st, combustion chamber；112nd, shock chamber；113rd, feed
Mouthful；114th, exhaust outlet；115th, through hole；116th, tedge；117th, low temperature synthesis gas entrance；118th, settler；119th, the first outlet
Mouthful；120th, slag-drip opening；20th, heat recovery unit；21st, heat exchanger；211st, the first housing；2111st, heat exchanging chamber；2112nd, gas outlet；
2113rd, air inlet；212nd, heat exchange unit；2121st, heat-transfer surface；2122nd, heat exchanger plates；2123rd, heat exchanger tube；2124th, mounting hole；213、
Doctor assemblies；2131st, scraper；214th, drive division；2141st, motor；2142nd, main shaft；215th, seal；22nd, cooling device；
221st, cooler；2211st, the second housing；2212nd, cooling chamber；2213rd, synthesis gas entrance；2214th, syngas outlet；222nd, first
Cyclone dust collectors；223rd, slag cooling component is scraped；224th, the first drum；225th, the second drum；2221st, shell；2222nd, first dirt is unloaded
Mouthful；2223rd, central tube；2224th, the second dust discharging port；2225th, guide；22251st, guide channel；2226th, cone；2227th, dedusting
Chamber；22271st, upper half chamber；22272nd, lower half chamber；2228th, through hole；2229th, dirt gap is unloaded；224th, the first drum；225th, the second vapour
Bag；30th, washing unit；31st, scrubbing tower；310th, the 3rd housing；311st, washing cavities；320th, down-comer；321st, the first straight length；
322nd, the second straight length；330th, spiral stream guidance blade；340th, spiral stream guidance passage；350th, scum pipe；360th, Venturi scrubber；
370th, solid valve type column plate；380th, scrubbing tower syngas outlet；390th, demister；32nd, water-gas conveyer；33rd, water-gas filters
Device；34th, water-gas separator；40th, usage on black water unit；41st, subsider；42nd, pond is ground；43rd, hp flash drum；44th, it is low
Press flash tank；45th, vacuum flasher；46th, cinder drier；47th, pond pump is ground；48th, ash water tank；49th, subsider underflow pump；
410th, band filter；50th, partially synthetic gas reflux unit；51st, the 8th pipeline；52nd, compressor；60th, the second cyclone dust collectors；
70th, ceramic filter；101st, the first pipeline；102nd, second pipe；103rd, the 3rd pipeline；104th, the 4th pipeline；105th, the 5th pipe
Road；106th, the 6th pipeline；107th, the 7th pipeline；108th, the 9th pipeline；109th, the tenth pipeline；110th, the 11st pipeline；100th,
12 pipelines；200th, control valve；10a, water-coal-slurry pipeline；11a, the first control valve；20a, the first nitrogen pipeline；21a, the second control
Valve processed；22a, the 3rd check (non-return) valve；30a, oxygen channel；301a, the first branch flow pipe；302a, the second branch flow pipe；31a, the 3rd
Control valve；32a, the 4th control valve；33a, the 5th control valve；34a, the 6th control valve；35a, the 4th pressure sensor；36a,
One regulating valve；37a, the first check (non-return) valve；38a, the second regulating valve；39a, the second check (non-return) valve；40a, the second nitrogen pipeline；401a、
First nitrogen branch flow pipe；402a, the second nitrogen branch flow pipe；403a, the 3rd nitrogen branch flow pipe；404a, the 4th nitrogen branch
Flow tube road；41a, the 4th check (non-return) valve；42a, the 7th control valve；43a, the 5th check (non-return) valve；44a, the 8th control valve；45a, the 6th stop
Inverse valve；46a, the 9th control valve；47a, the tenth control valve；48a, the 7th check (non-return) valve；50a, the 3rd nitrogen pipeline；51a, the 11st
Control valve；61a, first pressure sensor；62a, second pressure sensor；63a, the 3rd pressure sensor；70a, burner；81a、
First arithmetic device；82a, second arithmetic device.
Embodiment
Embodiments of the invention are described in detail below in conjunction with accompanying drawing, but the present invention can be defined by the claims
Implement with the multitude of different ways of covering.
Referring to shown in Fig. 1 to Figure 11, the coal-water slurry gasification system in the present invention includes：Feed unit, gasification unit
10 and heat recovery unit 20.Gasification unit 10 includes coal gasifier 11；Heat recovery unit 20 includes heat exchanger 21 and cooling
Device 22, wherein, the air inlet 2113 of heat exchanger 21 is connected with the first gas outlet 119 of coal gasifier 11, cooling device 22
Air inlet is connected with the gas outlet 2112 of heat exchanger 21, and heat exchanger 21 is respectively provided with heat exchanger tube, heat exchanger 21 with cooling device 22
Heat exchanger tube and cooling device 22 heat exchanger tube in be connected with cooling medium, the cooling medium fills to flowing through heat exchanger 21 and cooling
The heat for putting 22 synthesis gas carrying is reclaimed.During using coal-water slurry gasification system of the invention, lead to when by water-coal-slurry
After entering in coal gasifier 11, water-coal-slurry is handled and generated with CO and H through burning2Based on synthesis gas, now synthesis gas temperature
It is high, in 1350 degrees centigrades.Synthesis gas from coal gasifier 11 flow to heat exchanger 21 and cooling device 22 when, heat exchanger 21
Heat exchange is carried out between cooling medium and synthesis gas in the heat exchanger tube of heat exchanger tube and cooling device 22, so as to in synthesis gas
Heat is reclaimed.
The coal-water slurry gasification system mainly includes：
First, feed unit
Shown in Figure 1, the direction of arrow in figure represents the flow direction of the fluid in pipeline.Using the parking of the present invention
The coal gasifier feed unit of method specifically includes：
Water-coal-slurry pipeline 10a, water-coal-slurry pipeline 10a and coal gasifier burner 70a connections, on water-coal-slurry pipeline 10a
The first control valve 11a is provided with, first control valve 11a controls the break-make of water-coal-slurry pipeline；First nitrogen pipeline 20a, this
The second control valve 21a and the 3rd check (non-return) valve 22a is provided with one nitrogen pipeline 20a, wherein, the first nitrogen pipeline 20a and water coal
Pipeline 10a connections are starched, link position is located at the water-coal-slurry pipeline 10a duct section being connected with the first control valve 11a port of export
On, the 3rd check (non-return) valve 22a is arranged on the first nitrogen pipeline 20a and water-coal-slurry pipeline 10a link position and the second control valve 21a
Between duct section on.When the first control valve 11a is closed, the second control valve 21a is opened, into the first nitrogen pipeline 20a
It is passed through high pressure nitrogen, it is possible to the water-coal-slurry pipeline in water-coal-slurry pipeline 10a is purged to coal gasifier, and the 3rd check (non-return) valve
22a setting can then avoid fluid reflux in water-coal-slurry pipeline 10a in the first nitrogen pipeline 20a.
Coal gasifier feed system also includes oxygen channel 30a, oxygen channel 30a include the first branch flow pipe 301a and
Second branch flow pipe 302a, and the first branch flow pipe 301a is connected with the second branch flow pipe 302a with burner 70a.From oxygen hose
Road 30a charging aperture is on the pipeline of oxygen channel 30a forking node, being disposed with the 3rd control valve 31a, the 4th control
Valve 32a, the 5th control valve 33a.On oxygen channel 30a the first branch flow pipe 301a, once set along the flow direction of oxygen
Be equipped with the 6th control valve 34a, the first regulating valve 36a and the first check (non-return) valve 37a, and the 6th control valve 34a arrival end also
It is provided with the 4th pressure sensor 35a, the 6th control valve 34a of the pressure size of the first branch flow pipe 301a of detection porch
The aperture pressure that is detected according to the 4th pressure sensor 35a control.Use is additionally provided with the first branch flow pipe 301a
The second pressure sensor 62a of the pressure size of pipeline between the first check (non-return) valve 37a to burner 70a is detected, meanwhile, burner
First pressure the sensor 61a, first pressure sensor 61a and for the pressure size being provided with 70a in detection coal gasifier
Two pressure sensor 62a are connected with the first arithmetic device 81a of control system, and first arithmetic device 81a is to first pressure sensor
The result that 61a and second pressure sensor 62a are detected is calculated to control the first regulating valve 36a aperture.Second tributary
On pipeline 302a the second regulating valve 38a and the second check (non-return) valve 39a, the second check (non-return) valve are disposed with along the flow direction of oxygen
39a is to the 3rd pressure sensor 63a is provided with the pipeline between burner 70a, and the second arithmetic device 82a of control system is to first
The result that pressure sensor 61a and the 3rd pressure sensor 63a are detected is calculated to control opening for the second regulating valve 38a
Degree.
Coal gasifier feed system, which also includes the second nitrogen pipeline 40a, the second nitrogen pipeline 40a, includes the first nitrogen tributary
Pipeline 401a, the second nitrogen branch flow pipe 402a, the 3rd nitrogen branch flow pipe 403a and the 4th nitrogen branch flow pipe 404a, and
Four branch flow pipes are connected with oxygen channel 30a, by the oxygen blow in oxygen channel 30a to coal gasifier.Wherein,
First nitrogen branch flow pipe 401a and oxygen channel 30a link position be located at the 3rd control valve 31a and the 4th control valve 32a it
Between pipeline on, and on the first nitrogen branch flow pipe 401a along the flow direction of nitrogen be disposed with the 7th control valve 42a and
4th check (non-return) valve 41a；The link position of second nitrogen branch flow pipe 402a and oxygen channel is located at the 4th control valve 32a and the 5th
On pipeline between control valve 33a, and the 8th is disposed with along the flow direction of nitrogen on the second nitrogen branch flow pipe 402a
Control valve 44a and the 5th check (non-return) valve 43a；3rd nitrogen branch flow pipe 403a is connected with the second branch flow pipe 302a, and they it
Between link position be located on the pipeline that is connected with the second regulating valve 38a entrance point, and the 3rd nitrogen branch flow pipe 403a
On along the flow direction of nitrogen be disposed with the 9th control valve 46a and the 6th check (non-return) valve 45a；4th nitrogen branch flow pipe 404a
It is connected with the first branch flow pipe 301a, and their communicating position is between the 6th control valve 34a and the first regulating valve 36a
On pipeline, and the tenth control valve 47a and the 7th are disposed with along the flow direction of nitrogen on the 4th nitrogen branch flow pipe 404a
Check (non-return) valve 48a.
Shown in Figure 2, according to an embodiment of the invention, coal gasifier feed system control method for stopping is utilized above-mentioned
Coal gasifier feed system on the basis of realize, specifically include：Step S1：Stop to the burner of coal gasifier be passed through oxygen and
Water-coal-slurry；Step S2：The oxygen in oxygen channel is purged to coal gasifier by burner using nitrogen；Step S3：Keep
The water-coal-slurry in water-coal-slurry pipeline is purged to coal gasifier by burner to the purging state of oxygen channel, and using nitrogen
It is interior, after purging for first scheduled time to water-coal-slurry pipeline, stop the purging to water-coal-slurry pipeline；Step S4：Keep to oxygen hose
The purging state in road, and the pressure in oxygen channel is more than the pressure in coal gasifier, it is predetermined to oxygen channel purging second
After time, stop the purging to oxygen channel；Step S5：Pressure release is carried out to coal gasifier.According to an embodiment of the invention, entirely
In docking process, because the pressure in oxygen channel 30a is more than the pressure in gasification furnace, the synthesis in gasification furnace can be effectively avoided
Gas, which carries pulverized coal particle and plays a reversed role to be formed in oxygen channel 30a, dodges quick-fried phenomenon, while avoids excessive coal ash from being burnt into burner
Adhered to inside mouth, enable its premium properties of the holding of burner longer time.It should be noted that nitrogen described in the present embodiment
Gas, its pressure are more than the pressure of the oxygen in oxygen channel 30a.In the present embodiment, the purging nitrogen in water-coal-slurry pipeline 10a
Be same source nitrogen with the purging nitrogen in oxygen channel 30a, pressure is equally high, is high pressure nitrogen, it is general we by pressure
Nitrogen higher than 8.0MPa is referred to as high pressure nitrogen.
Coal gasifier feed system with reference to shown in Figure 11 illustrates the operating process of each step.Before parking, the
One control valve 11a, the 3rd control valve 31a, the 4th control valve 32a, the 5th control valve 33a, the 6th control valve 34a, the first regulation
Valve 36a and the second regulating valve 38a are in open mode, and remaining control valve is in closed mode.
In step sl, the first control valve 11a, the 3rd control valve 31a are closed, stops leading to the burner 70a of coal gasifier
Enter water-coal-slurry and oxygen, and then stop being passed through water-coal-slurry and oxygen into coal gasifier.
Then step S2 is carried out, opens the 7th control valve 42a, the 8th control valve 44a, the 9th control valve 46a and the tenth
Control valve 47a, and high pressure nitrogen is passed through into the second nitrogen pipeline 40a, by the oxygen blow in oxygen channel 30a to coal gasification
In stove.
Then step S3 is carried out, the second control valve 21a is opened, high pressure nitrogen is passed through into the first nitrogen pipeline 20a, is utilized
High pressure nitrogen is purged to water-coal-slurry pipeline 10a, and the water-coal-slurry in water-coal-slurry pipeline 10a is purged into coal gasifier, is protected
After holding purging 12S, the second control valve 21a is closed, now, the water-coal-slurry in water-coal-slurry pipeline 10a is purged to coal gas completely
Change in stove, in other embodiments of the invention, shape can also be used according to reality to water-coal-slurry pipeline 10a purge time
Condition is adjusted, but oxygen channel 30a purge time must be longer than water-coal-slurry pipeline 10a purge time.
Then step S4 is carried out, due in whole coal gasifier feed system, potential safety hazard highest position is positioned at the
Three control valve 31a are in this section of oxygen channel of burner 70a, as long as therefore ensureing that synthesis gas will not carry coal ash from coal gasification
Stove is played a reversed role to the security that can ensure whole system in the first branch flow pipe 301a and the second branch flow pipe 302a.Therefore, exist
In step S4, the pressure in the first branch flow pipe 301a is more than the pressure in coal gasifier first, ensure in coal gasifier
Coal dust will not play a reversed role into the first branch flow pipe 301a.
Preferably, in the present embodiment, the first check (non-return) valve 37a and the first regulating valve are provided with the first branch flow pipe 301a
36a, the first regulating valve 36a, the first check (non-return) valve 37a and the first regulating valve 36a are set gradually along the direction away from burner 70a；The
Second pressure sensor 62a is additionally provided with one branch flow pipe 301a, it is non-return that second pressure sensor 62a is used for detection first
The pressure in duct section between valve 37a to burner 70a；The first pressure for the pressure being provided with gasification furnace in detection gasification furnace
Sensor 61a；In step s 4, the pressure that control system detects according to first pressure sensor 61a and second pressure sensor 62a
The magnitude relationship of force value and the pressure difference of setting automatically adjust the first regulating valve 36a aperture, so that the first check (non-return) valve 37a is to burning
The pressure in duct section between mouth 70a is more than the pressure in gasification furnace, avoids the coal dust in coal gasifier from playing a reversed role to first
In flow tube road 301a.
Preferably, control system includes first arithmetic device 81a, first arithmetic device 81a to first pressure sensor 61a and
The pressure value of second pressure sensor 62a detections carries out computing, compares the pipeline between the first check (non-return) valve 37a to burner 70a
Pressure difference in section in pressure gentleization stove, and then the first regulating valve 36a aperture is controlled to ensure the first check (non-return) valve 37a to burning
Duct section internal pressure between mouth 70a is powerful in pressure in gasification furnace, avoids playing a reversed role for coal dust, improves the security of system.It is more excellent
Selection of land, in step s 4, the pressure difference in the pressure and gasification furnace in duct section between the first check (non-return) valve 37a to burner 70a
In the range of 0.01MPa to 0.03MPa, i.e. the pressure in duct section between the first check (non-return) valve 37a to burner 70a compares coal gas
Change the pressure high 0.01MPa to 0.03MPa in stove.On the one hand avoid the coal dust in coal gasifier from playing a reversed role to return in oxygen channel,
On the other hand pressure difference can also be avoided excessive and produce potential safety hazard, in other embodiments of the invention, the value of pressure difference
Can also suitably it be changed according to the behaviour in service of reality.
According to the coal gasifier feed system of the present invention it is recognised that oxygen channel 30a includes the second branch flow pipe 302a,
Second branch flow pipe 302a is connected with burner 70a, in step s 4, the pressure in the second branch flow pipe 302a is more than coal gasification
Pressure in stove, further improve the security of whole system.
Preferably, in the present embodiment, the second check (non-return) valve 39a and the second regulating valve are provided with the second branch flow pipe 302a
38a, the second check (non-return) valve 39a and the second regulating valve 38a are set gradually along the direction away from burner 70a；Second branch flow pipe 302a
On be additionally provided with the 3rd pressure sensor 63a, the 3rd pressure sensor 63a be used to detecting the second regulating valve 38a to burner 70a it
Between duct section in pressure；In step s 4, control system is according to first pressure sensor 61a and the 3rd pressure sensor
The magnitude relationship of the pressure value of 63a detections and the pressure difference of setting automatically adjust the second regulating valve 38a aperture, so that second stops
The pressure in duct section between inverse valve 39a to burner 70a is more than the pressure in coal gasifier, avoids the coal dust in coal gasifier
Play a reversed role into the first branch flow pipe 301a, further improve the security of whole system.
Preferably, control system includes second arithmetic device 82a, and second arithmetic device 82a is to first pressure sensor 61a and
The pressure value of three pressure sensor 63a detections carries out computing, compares the duct section between the second check (non-return) valve 39a to burner 70a
Pressure difference in interior pressure and coal gasifier, so control the second regulating valve 38a aperture with ensure the second check (non-return) valve 39a to burning
Duct section internal pressure between mouth 70a is powerful in pressure in coal gasifier, avoids playing a reversed role for coal dust, improves the security of system.More
Preferably, in step s 4, pressure and the pressure in gas Coalification furnace in the duct section between the second check (non-return) valve 39a to burner 70a
For difference in the range of 0.01MPa to 0.03MPa, i.e. the pressure in duct section between the second check (non-return) valve 39a to burner 70a compares coal
Pressure high 0.01MPa to 0.03MPa in gasification furnace.On the one hand avoid the coal dust in coal gasifier from playing a reversed role and return to oxygen channel
In, pressure difference on the other hand can also be avoided excessive and produce potential safety hazard, in other embodiments of the invention, pressure difference
Value can also suitably be changed according to the behaviour in service of reality.
After step S4 operation 15S is kept, the 4th control valve 32a, the 7th control valve 42a, the 8th control valve are closed
44a, stop the purge to oxygen channel 30a.
Then step S5 is carried out, burner 70a is carried out in pressure discharge operations pressure leak process, pressure release speed is less than 0.1MPa/
Min, the inner parts structure for avoiding pressure release too fast and damaging in coal gasifier.Typically when gasification furnace pressure is less than 0.4MPa, visually
Terminate for pressure release.After pressure release terminates, the 9th control valve 46a and the tenth control valve 47a are closed, and stop leading to oxygen channel 30a
Enter high pressure nitrogen.First arithmetic device 81a and second arithmetic device 82a continue to come into operation, the first regulating valve 36a and the second regulating valve 38a
Continue respectively by first arithmetic device 81a and second arithmetic device 82a operation result, aperture is controlled by control system to adjust the
First, the pressure difference in two check (non-return) valves to pressure in the duct section between burner 70a and gas Coalification furnace is in 0.01MPa to 0.03MPa
In the range of.
Also include step S6 after step s 5：After pressure release terminates, between the first check (non-return) valve 37a to burner 70a of holding
Pressure in duct section is more than the pressure in coal gasifier, and keeps in the duct section between the second check (non-return) valve 39a to burner 70a
Pressure be more than pressure in coal gasifier, until oxygen channel 30a and water-coal-slurry pipeline 10a are removed from burner 70a.I.e.
It relative to the pressure in coal gasifier is pressure-fired to keep the pressure between first and second check (non-return) valve and burner 70a in oxygen channel,
Prevent gasification furnace gas from carrying dust and playing a reversed role or nitrogen will be full of in coal gasifier, carried out fully using coal gasifier for next time
Prepare, avoid driving next time being to occur dodging quick-fried phenomenon.Concrete operations are：When the 9th control valve 46a and the tenth control valve 47a is closed
After closing, the 11st control valve 51a on the 3rd nitrogen pipeline 50a is opened immediately, i.e., high pressure nitrogen is switched into low-pressure nitrogen, after
It is continuous to continue to be passed through low-pressure nitrogen to oxygen channel, keep it to be full of nitrogen state, persistently keep the pressure in oxygen channel 30a big
In the pressure in coal gasifier, until oxygen channel 30a and water-coal-slurry pipeline 10a are removed from burner 70a.Water-coal-slurry pipeline
After 10a and oxygen channel 30a is split out from burner 70a, after the flange port that oxygen channel connects with burner is sealed, you can close
11st control valve 51a stops being passed through nitrogen.Described low-pressure nitrogen is the nitrogen that pressure is less than 0.8MPa in the present embodiment, is protected
The pressure between first and second check (non-return) valve and burner 70a in oxygen channel is demonstrate,proved slightly larger than the pressure in coal gasifier, prevents gasification furnace
The coal dust that interior synthesis gas carries is played a reversed role.
2nd, gasification unit 10, mainly coal gasifier 11 is included.Gasification process is carried out to water-coal-slurry using coal gasifier 11.
(1) coal gasifier 11
Referring to shown in Fig. 1 and Fig. 2, coal gasifier 11 includes body of heater, and the body of heater includes combustion chamber 111, shock chamber 112, entered
Material mouth 113 and exhaust outlet 114, wherein, shock chamber 112 is arranged on the lower section of combustion chamber 111, and the bottom of combustion chamber 111 is opened
Provided with the through hole 115 connected with shock chamber 112；Charging aperture 113 is arranged on body of heater, and is connected with combustion chamber 111；Exhaust outlet
114 are arranged on the top of combustion chamber 111, and are connected with combustion chamber 111.Do not set in the shock chamber 112 of whole coal gasifier 11
The inner parts structures such as down-comer are put, are directly connected between combustion chamber 111 and shock chamber 112, when coal gasifier 11 works, water
Coal slurry and oxygen enter combustion chamber 111 from charging aperture 113, and remaining molten state lime-ash directly passes through through hole after burning processing
115 drop into the water cooling solidification of the bottom of shock chamber 112, because the bottom of shock chamber 112 is the water-bath with certain liquid level, because
Water-bath separates the slag-drip opening of the inner chamber of shock chamber 112 and its bottom, so the inner chamber of shock chamber 112 forms a closed chamber,
Now burning is caused by CO in combustion chamber 1112, CO and H2The crude synthesis gas of formation is then from being arranged on the upper end of combustion chamber 111
Exhaust outlet 114 is discharged to outside combustion chamber 111, and then realizes the function of opening synthesis gas and lime-ash initial gross separation, it is seen then that is adopted
Can realize the conventional aerogenesis function of coal gasifier 11 with the coal gasifier 11 of the present invention, and and down-comer need not be set and swashed
The internals such as cold ring, so as to avoid the phenomenon that the internals damage of shock chamber 112 causes parking accident frequently to occur, improve coal gasification
The service life of stove 11 and stability.
The communicating position of charging aperture 113 and combustion chamber 111 is located on combustion chamber 111, and in charging aperture 113 close to combustion chamber
111 opening position sets nozzle, and in the present embodiment, nozzle is linked together with charging aperture integration in fact, into burning
The oxygen for the high speed and high pressure that the water-coal-slurry of room 111 is injected into is dispelled and is atomized.Preferably, the charging aperture 113 in the present embodiment is
Even number, such as 4,6,8 etc., and the even number charging aperture 113 is symmetrical arranged two-by-two along the circumference of combustion chamber 111, and now, phase
The water-coal-slurry that symmetrical two nozzles spray mutually is hit broken, is reached more preferable atomizing effect and more preferably gasification efficiency, is entered
And improve gasification efficiency of the water-coal-slurry in combustion chamber 111.
Coal gasifier 11 also includes the tedge 116 for being arranged on the top of body of heater, and the tedge 116 and exhaust outlet 114 are right
Connect and extend along the direction away from combustion chamber 111.Because water-coal-slurry can produce lime-ash not of uniform size during burning, lead to
In the case of often, most of lime-ash can sink and be cooled down by through hole 115 into shock chamber 112, however, a part of particle shape
Lime-ash can then follow crude synthesis gas (main component CO2, CO and H2) discharge combustion chamber 111.To connecting on exhaust outlet 114
After tedge 116, in crude synthesis gas the lime-ash of larger particles shape because its density it is larger under gravity in tedge 116 on
Lifting speed tapers into and then stops rising, and then reversely slowly sinks, is again introduced into combustion chamber 111, finally sinks to shock chamber
Cooled and solidified in 112 entrance water-baths, the downstream for entering coal gasifier 11 together so as to avoid excessive lime-ash with synthesis gas fills
In putting, by the lime-ash of cooling and solidifying, finally total slag-drip opening 120 flows out coal gasifier 11.
Preferably, the body of heater in the present embodiment is column structure, and tedge 116 is straight tube, ensures that synthesis gas circulation is smooth
Also settlement space is provided while property for the backflow of lime-ash.And tedge 116, through hole 115 and row in the present embodiment
Gas port 114 is arranged along the central axis of column structure, further ensures the patency of synthesis gas and lime-ash flowing.
Preferably, coal gasifier 11 also includes settler 118, and settler 118 is arranged on the remote combustion chamber of tedge 116
111 one end, and the settler 118 has cushion chamber, cushion chamber connects with tedge 116, slow to being entered from tedge 116
The synthesis gas for rushing intracavitary carries out buffered, and the internal diameter of the cushion chamber of settler 118 is bigger than the internal diameter of tedge 116, enters
Crude synthesis gas flow velocity slows down so that the ability that crude synthesis gas carries solid particle dies down, grey so as to be more beneficial in crude synthesis gas
Slag settles down.Specifically, in tedge 116, gas-solid obtains initial gross separation, when synthesis gas enters the settler of major diameter
In 118, flow velocity declines rapidly, and the grey solid impurity particle in part also slows down and rises and then fall therewith, further gas solid separation.
According to the present embodiment, after synthesis gas and separated lime-ash, synthesis gas should be discharged to whole coal gasifier 11,
Therefore, the first gas outlet 119 is additionally provided with coal gasifier 11, first gas outlet 119 is arranged on the remote of settler 118
One end of tedge 116, and connected with cushion chamber, so as to which coal gasifier 11 will be discharged by the synthesis gas after gas solid separation.
Preferably, the liner of heat resistant and wear resistant is provided with the inwall of the tedge 116 in the present embodiment and cushion chamber
Layer, avoids settler 118 and tedge from being washed away by particle, to improve the service life of whole coal gasifier 11.
During coal water slurry gasification, the downstream of coal gasifier 11 is provided with Slag Scraping Device and deduster etc. and set, and from
The extreme temperatures for the synthesis gas that combustion chamber 111 comes out, about 1300 degrees Celsius, and its easily cause heat etching to damage upstream device,
Therefore, low temperature synthesis gas entrance 117 is additionally provided with coal gasifier 11, the low temperature synthesis gas entrance 117 is arranged on tedge
Connected on 116 and with tedge 116, when being passed through low temperature synthesis gas at low temperature synthesis gas entrance 117, the low temperature synthesis gas can be with
The high-temperature synthesis gas mixing discharged from combustion chamber 111, so as to reduce the temperature for the synthesis gas for entering coal synthesizer downstream.This
When, upstream device on the one hand can be protected by high temperature failure, on the other hand can also reduce the economic input amount of the equipment in downstream,
The cost of enterprise is greatly saved.
3rd, heat recovery unit 20, it is connected with gasification unit 10, to handling the synthesis gas formed afterwards through coal gasifier 11
Handled, reclaim the heat entrained by synthesis gas.The heat recovery unit 20 mainly include heat exchanger 21, cooling device 22,
And second cyclone dust collectors 60.The air inlet 2113 of heat exchanger 21 is connected with the first gas outlet 119 of coal gasifier 11, cooling
The air inlet of device 22 is connected with the gas outlet 2112 of heat exchanger 21, and heat exchanger 21 is respectively provided with heat exchanger tube with cooling device 22,
The heat exchanger tube of heat exchanger 21 in the heat exchanger tube of cooling device 22 with being connected with cooling medium, and the cooling medium is to flowing through heat exchanger 21
The heat carried with the synthesis gas of cooling device 22 is reclaimed.
(1) heat exchanger 21
With reference to shown in Fig. 1 Fig. 3 to Fig. 5, according to an embodiment of the invention, heat exchanger 21 includes：First housing 211, heat exchange
Unit 212, doctor assemblies 213 and drive division 214, wherein, the first housing 211, which encloses, to be set to form heat exchanging chamber 2111；Heat exchange unit
212 and doctor assemblies 213 be arranged in heat exchanging chamber 2111；Drive division 214 drives doctor assemblies 213 to scrape heat exchange unit 212
On lime-ash.According to an embodiment of the invention, under the driving of drive division 214, doctor assemblies 213 can be by heat exchange unit 212
On lime-ash scrape, avoid lime-ash from being deposited in heat exchanging chamber 2111 and cause the obstruction of heat exchanger, effectively increase heat exchanger
Heat transfer effect.
Preferably, heat exchange unit 212 is multiple that can effectively improve the heat transfer effect of heat exchanger.In other embodiments,
Heat exchange unit 212 can also be one.According to the present embodiment, each heat exchange unit 212 includes heat-transfer surface 2121, doctor assemblies
213 be multiple, and multiple doctor assemblies 213 are set correspondingly with multiple heat-transfer surfaces 2121, under the driving of drive division 214,
Doctor assemblies 213 move in the region close to heat-transfer surface 2121, will scrape the lime-ash on heat-transfer surface 2121.
Preferably, multiple heat exchange units 212 side by side and are arranged at intervals, and keep the heat exchange of two neighboring heat exchange unit 212
Face 2121 is relative.Specifically, each heat exchange unit 212 includes two heat-transfer surfaces 2121, when multiple heat exchange units 212 side by side between
When setting, gap is formed between relative two heat-transfer surfaces 2121, heat exchange processing is carried out to the fluid for flowing through gap.
In the present embodiment, multiple heat exchange units 212 form a plurality of heat exchange gap, after fluid enters heat exchanger, be divided into multiply and
Into gap, the heat exchange efficiency of heat exchanger is effectively increased.
Preferably, drive division 214 includes motor 2141, and the main shaft 2142 of motor 2141 is single through multiple heat exchange
Member 212, doctor assemblies 213 are fixedly installed on main shaft 2142, during heat exchanger works, when motor 2141 rotates
When, the doctor assemblies 213 being arranged on main shaft 2142 on the one hand can be driven to rotate, so as to scrape the ash on heat exchange unit 212
Slag, on the other hand, the motion of doctor assemblies 213 can change the movement locus of the lime-ash in heat exchanging chamber 2111, make lime-ash in sky
Interior motion becomes more active, and then prevents the deposition of lime-ash.
In the present embodiment, doctor assemblies 213 include more scraper 2131, it is more scraper 2131 along the same of main shaft 2142
It is arranged circumferentially, and multiple scrapers 2131 are each perpendicular to main shaft 2142, it is more scraper 2131 when main shaft 2142 rotates
It can be moved in the region close to heat-transfer surface 2121, scrape the lime-ash on heat-transfer surface 2121, and effectively improve scraping for lime-ash
Rate.
Preferably, motor 2141 is arranged on the outside of the first housing 211, easy to operation and control.Each heat exchange unit
212 middle part is provided with mounting hole 2124, and the main shaft 2142 of motor 2141 stretches into heat exchanging chamber 2111 and runs through each peace
Hole 2124 is filled, now, multiple doctor assemblies 213 is driven with a can of motor 2141, greatlys save heat exchanger
Manufacturing cost.It is highly preferred that the main shaft 2142 of motor 2141 is close with being provided with the contact position of the first housing 211
Sealing 215, prevent main shaft 2142 from producing leakage in the opening position contacted with the first housing 211.
Referring again to shown in 3 and Fig. 5, heat exchange unit 212 also includes polylith heat exchanger plates 2122 and heat exchanger tube 2123, and polylith changes
Hot plate 2122, which encloses, is set as cuboid installing space；Heat exchanger tube 2123 is arranged in installing space.According to the present embodiment, heat exchanger tube
2123, which are arranged on polylith heat exchanger plates 2122, encloses in the installing space being set as, and increases the heat exchange area of heat exchange unit 212, improves whole
The heat transfer effect of heat exchanger, and be easily installed.It is highly preferred that heat exchanger tube 2123 is arranged in installing space in wavy, increase
The length of heat exchanger tube 2123, so as to add the cooling medium in heat exchange unit 212, further improve the heat exchange effect of heat exchanger
Fruit.In the present embodiment, the both ends of heat exchanger tube 2123 stretch out heat transfer space and reach the outside of the first housing 211, and being easy to will be cold
But the heat exchanging chamber 2111 of heat exchanger is sent into or excluded to medium.
According to an embodiment of the invention, synthesis gas gas outlet 2112 and air inlet 2113 are provided with the first housing 211, and
Gas outlet 2112 and air inlet 2113 are oppositely arranged so that the lime-ash scraped by doctor assemblies 213 can flow together with fluid
Go out the heat exchanging chamber 2111 of heat exchanger.Gas outlet 2112 and air inlet 2113 can not also relatively, as long as protecting in other embodiments
Fluid and lime-ash in card heat exchanging chamber 2111 can be excluded heat exchanging chamber 2111.
Preferably, heat-transfer surface 2121 is parallel to gas outlet 2112 and the axis of air inlet 2113, namely adjacent two
Gap between heat exchange unit 212 is further ensured that by scraper parallel to the line between gas outlet 2112 and air inlet 2113
The lime-ash that component 213 scrapes can swimmingly discharge the heat exchanging chamber 2111 of heat exchanger together with the fluid to be exchanged heat, prevent ash
Slag is deposited on the outer surface of heat exchange unit 212 again when around heat exchange unit 212.
(2) cooling device 22, the cooling device 22 include cooler 221, the first cyclone dust collectors 222 and multiple scrape slag
Cooling component 223.Cooler 221 includes cooling chamber 2212, synthesis gas entrance 2213 and syngas outlet 2214, and synthesis gas enters
Mouth 2213 forms the air inlet of cooling devices 22；First cyclone dust collectors 222 are arranged on the syngas outlet 2214 of cooler 221
Place, and the import of the first cyclone dust collectors 222 connects with the syngas outlet 2214 of cooler 221, the first cyclone dust collectors 222
Export mixes cooling device 22 gas outlet；Multiple length direction arrangements for scraping slag cooling component 223 along cooling chamber 2212, and
Respectively scrape slag cooling component 223 and be respectively provided with heat exchanger tube.During work, synthesis gas enters from the air inlet of cooling device 22, in cooling chamber
Cooled down in 2212, and heat recovery is carried out by heat exchanger tube, then from the first rotation after the dedusting of the first cyclone dust collectors 222
The outlet of the outlet of wind deduster 222, i.e. cooling device 22 excludes cooling device 22.
With reference to shown in Fig. 6, the cooling device includes cooler 221, and the cooler 221 includes the second housing 2211, multiple
Slag cooling component 223 is scraped, sets to form cooling chamber 2212 wherein the second housing 2211 encloses, the top of cooling chamber 2212 is provided with synthesis
Gas entrance 2213, the bottom of cooling chamber 2212 are provided with syngas outlet 2214, and synthesis gas entrance 2213 forms cooling device 22
Air inlet；Multiple length direction arrangements for scraping slag cooling component 223 along cooling chamber 2212, cooling chamber 2212 is flowed through for cooling down
Interior high-temperature synthesis gas simultaneously reclaims the heat entrained by high-temperature synthesis gas, and it is multiple scrape slag cooling component 223 be additionally operable to scrape it is cold
But the lime-ash in chamber 2212.According to an embodiment of the invention, when synthesis gas enters cooling chamber 2212 from synthesis gas entrance 2213,
Scrape the one side of slag cooling component 223 along what the length direction of cooling chamber 2212 was arranged and can carry out multistage cooling to synthesis gas, separately
On the one hand its scraper can effectively scrape the lime-ash for being attached to heat exchanger surface, scratch or puncture the bulk fallen from cooling chamber 2212
Slag.The lime-ash scraped can flow into cyclone dust collectors with synthesis gas from the synthesis outlet of the bottom of cooling chamber 2212, remove and close
Into the lime-ash in gas.It can be seen that cooling device of the invention can not only improve the rate of recovery to the heat of high-temperature synthesis gas, and
It is not easy the blocked phenomenon of cooler 221 occur, substantially increases the cycle of device stable operation, reduce cost and improve
Benefit.
In the present embodiment, scrape that structure and the structure of heat exchanger 21 of slag cooling component 223 are essentially identical, and difference exists
In, scrape slag cooling component 223 and be not provided with the first housing 211, but directly by heat exchange unit 212, the doctor assemblies of heat exchanger
213 and drive division 214 be arranged on cooler 221.Specific installation site is shown in Figure 6.
The cooling device of the present embodiment also includes the first drum 224 and the second drum 225, wherein the first drum 224 and
Two drums 225 are arranged at outside the second housing 2211.And scrape slag cooling component 223 (can want for three according to specific heat exchange
Ask and set some to scrape slag heat exchanger in cooling chamber, be not necessarily three), three first scraped in slag cooling component 223
With the 3rd, namely scrape close to one of synthesis gas entrance 2213 slag cooling component 223 and close to syngas outlet 2214 one
Individual slag cooling component 223 of scraping is connected with the first drum 224；Centrally located scrapes the drum of slag cooling component 223 and second
225 connections.
In the present embodiment, slag cooling component 223 is scraped successively to cold along what the length direction of cooling chamber 2212 was set gradually
But the synthesis gas in chamber 2212 is cooled down, and carries out heat exchange, is closed using the cooling medium in slag cooling component 223 is scraped to absorb
Into the heat entrained by gas, in this process, the temperature of synthesis gas is successively decreased step by step, can be by the first drum 224 and
Cooling water in two drums 225 is changed into the different steam of temperature, using these steam, can also be carried out available for driving equipment secondary
Heat exchange, it is seen then that the cooling device of the present embodiment to the heat that synthesis gas carries can reclaim and utilize again, greatly improve
The efficiency of enterprise simultaneously avoids the loss of energy.
Specifically, the first drum 224 scrapes slag cooling component 223 built with cooling water, close syngas outlet 2214,
The entrance of i.e. first heat exchanger tube for scraping slag cooling component 223 is connected by the first pipeline 101 with the first drum 224, the first pipe
The first end of road 101 is arranged on the bottom of the first drum 224；Slag cooling component 223, i.e., the 3rd are scraped close to syngas outlet 2214
The outlet of the individual heat exchanger tube for scraping slag cooling component 223 is connected by second pipe 102 with the first drum 224, second pipe 102
One end is arranged on the top of the first drum 224；The entrance for scraping slag cooling component 223 close to syngas outlet 2214 is by the 3rd
Pipeline 103 is connected with the first drum 224, and the first end of the 3rd pipeline 103 is arranged on the top of the first drum 224.In the course of work
In, when needing to cool down the synthesis gas in cooling chamber 2212, the cooling water in the first drum 224 passes through the first pipeline
101 flow in each heat exchanger tube for scraping slag cooling component 223 of syngas outlet 2214, with the synthesis in cooling chamber 2212
Gas carries out heat exchange heat and produces steam, and steam flows out from heat exchanger tube, and flow to the first drum from by second pipe 102
224 top, and it is centrally located scrape slag cooling component 223, i.e. second heat exchanger tube for scraping slag cooling component 223 enters
Mouth is connected by the 4th pipeline 104 with the second drum 225, and the first end of the 4th pipeline 104 is arranged on the bottom of the second drum 225
Portion；The outlet of the centrally located heat exchanger tube for scraping slag cooling component 223 is connected by the 5th pipeline 105 and the second drum 225
Connect, and the first end of the 5th pipeline 105 is arranged on the top of the second drum 225.During heat exchange is carried out, cooling water from
4th pipeline 104 is flowed into the heat exchanger tube for scraping slag cooling component 223 in centre position, is carried out in cooling chamber 2212 with synthesis gas
Heat exchange type from the 5th pipeline 105 into flowing out after steam, and the entrance of the heat exchanger tube of heat exchanger 21 passes through the 6th pipeline 106 and
Two drums 225 connect, and the first end of the 6th pipeline 106 is arranged on the top of the second drum 225.Now, in the second drum 225
Steam more than liquid level can be entered in the 6th pipeline 106, entered in the heat exchanger tube of heat exchanger 21, in heat exchanging chamber 2111 with
Synthesis gas flows out after carrying out heat exchange from the port of export of the heat exchanger tube of heat exchanger 21, it is possible to which the thermal high of crossing for obtaining high-quality steams
Vapour.
Cooling chamber 2212 is vertically arranged in the present invention, the cyclone dust collectors 222 of syngas outlet 2214 and first of its bottom
It is connected, is advantageous to the gas solid separation operation of the deduster of bottom connection, so as to obtain more preferable dust removing effects.
The inwall of cooling chamber 2212 is provided with Wear-resistant, high-temperature resistant and heat-insulating material, to prevent solid particle in synthesis gas
Wash away and wear, and synthesis gas heat scatter and disappear；Because synthesis gas temperature is very high, scrapes slag cooling component 223 and be arranged on cooling chamber
Inside 2212, it can effectively reduce heat and scatter and disappear and lose, cooling cavity structure is simple, and manufacturing cost is not high.In other of the present invention
In embodiment, two or more cooling chambers 2212 can be set according to being actually needed, during production, one comes into operation, a work
To be standby, so it is (standby that the cooling chamber 2212 of the failure of operation can be cut out into maintenance in the case where gasification furnace is not parking
Come into operation), add the flexibility of production operation, avoid parking caused by economic loss.
The cooling device 22 of the present embodiment also includes the first cyclone dust collectors 222, and first cyclone dust collectors 222 are arranged on
At the syngas outlet 2214 of the bottom of cooler 221, dedusting is carried out to the synthesis gas with lime-ash of slave synthesizer outflow.
Specifically, the first cyclone dust collectors 222 include shell 2221, central tube 2223, guide 2225 and cone
2226, wherein, shell 2221, which encloses, to be set to form dedusting chamber 2227, and the bottom of dedusting chamber 2227 is provided with the first dust discharging port 2222；
Central tube 2223 is arranged in dedusting chamber 2227, and the upper port of central tube 2223 extends to the outer of dedusting chamber 2227
Portion, and upper port is connected with syngas outlet 2214, is easy to the synthesis gas after cooler 221 to enter cyclone dust collectors, center
The lower port of pipe 2223 is the second dust discharging port 2224, and the second dust discharging port 2224 extends to the first dust discharging port 2222, in exclusion
The outside that the solid particle to get off is rejected to dedusting chamber 2227 is deposited in heart pipe 2223；
Guide 2225 is arranged in dedusting chamber 2227, and the medial extremity of guide 2225 and 2223 tangent company of central tube
Connect, when synthesis gas flows out from guide channel 22251, accumulate the air-flow of one corkscrew motion, so, gravity and from
In the presence of mental and physical efforts, it is easy to separate solid particle entrained in effective synthesis gas and synthesis gas, guide 2225
Outboard end stretches out away from central tube 2223, has guide channel 22251 on guide 2225, guide channel 22251 is with
Heart pipe 2223 connects；
In the centrally disposed pipe 2223 of cone 2226, installation site of the cone in central tube 2223 is less than guide channel
22251 are positioned close to the side of communicating position and are located at central tube with the communicating position of central tube 2223, the cone of cone
It is used to preventing that solid particle in central tube 2223 from disturbing and/or a large amount of synthesis gas are from the second dust discharging port on 2223 axis
2224 outflows.
Formed between the inwall of the margin and center pipe 2223 of the bottom surface of cone 2226 and unload dirt gap 2229, be easy to center
Lime-ash in pipe 2223 excludes.When cone 2226 is arranged below the communicating position of guide channel 22251 and central tube 2223, one
Aspect can separate the solid particle at dust discharging port and the synthesis gas flowed out from guide channel 22251, on the other hand can also
A large amount of synthesis gas are avoided to be gone out from dust discharging port.When synthesis gas, the upper port of pipe 2223 is entered fashionable centered on, and synthesis gas is therefrom
The upper port of heart pipe 2223 flows downward, and solid particle flows downward therewith under the entrainment of synthesis gas, most of solid particle
Hit and slide (effect for also functioning to inertial dust collection) from unloading dirt gap 2229 after cone 2226 or the inwall of central tube 2223, and from the
Flowed out in two dust discharging ports 2224, and synthesis gas meets the guide channel after cone 2226 stops after reverse flow from guide 2225
22251 spirally flow out.
Preferably, dedusting chamber 2227 includes upper half chamber 22271 and lower half chamber 22272, is provided with shell 2221 and upper half
Chamber 22271 is tangent and the row of the synthesis gas in the first cyclone dust collectors 222 is easy in the through hole 2228 of connection, the setting of through hole 2228
Go out.The bottom of lower half chamber 22272 in the present embodiment is in funnel-shaped structure, and the first dust discharging port 2222 is located at funnel-shaped structure most
At lower position, the lower port of the close lower half chamber 22272 of pipe 2223 centered on the second dust discharging port 2224, it is easy to the row of solid particle
Put.
Preferably, the volume of upper half chamber 22271 is less than the volume of lower half chamber 22272, and central tube 2223 runs through upper half chamber
22271 and lower half chamber 22272, in this configuration, when synthesis gas is in upper half chamber 22271, flow velocity is fast, there is provided
To the efficiency of dust collection of synthesis gas, and when synthesis gas enters in lower half chamber 22272, because cushion space is big, synthesis gas
Flows decrease, it is easy to the deposition of solid particle, effectively increases dust removing effects.And guide 2225 is arranged on lower half chamber 22272
Interior, when synthesis gas flows out into lower half chamber 22272 from guide channel 22251, now, the synthesis gas of outflow can be in lower half chamber
22272 and upper half chamber 22271 in form helical flow, in the presence of gravity and centrifugal force, fraction solids particle is thrown to down
Slid after half chamber 22272 and the inwall of upper half chamber 22271, dedusting again, after removing dust, synthesis gas gas is from the row of through hole 2228
Go out, solid particle is then discharged from the first dust discharging port 2222 of the bottom of lower half chamber 22272.Preferably, the bottom of lower half chamber 22272 is in
Funnel-shaped structure, the first dust discharging port 2222 are located at its lowest position of funnel-shaped structure, are easy to the discharge of solid particle.
Preferably, guide 2225 is multiple, multiple guides 2225 along central tube 2223 be arranged circumferentially and position
When the fooled synthesis gas of the sustained height of central tube 2223 enters central tube 2223, screw can be formed, is easy to synthesize
Solid particle and gas in gas separate.
In the present embodiment, guide 2225 is square guide pad, and guide channel 22251 is to be arranged on square guide pad
Guiding gutter, guiding gutter is recessed from the low side of square guide pad to top, and from the remote central tube 2,223 1 of square guide pad
Side is through to close to the side of central tube 2223.When being directed to part 2225 and being arranged to square guide pad, guiding gutter can be set
Relatively narrower, so, not only have the function that certain inertial dust collection due in movement air flow grit have from gas it is different
Inertia force, when dusty gas takes a sudden turn or collided with certain barrier, the movement locus of grit will be separated, and cause
Synthesis gas is formed under the long and narrow guide effect of guide channel 22251 with certain orientation and the stronger air-flow of directionality, these from
It is all tangent with the circumference of central tube 2223 to open the direction of the air-flow of respective guide channel 22251, now, these leave each self- steering and led to
The air-flow in road 22251 accumulates the air-flow of one corkscrew motion again, and this strand of spiral air flow formed under this structure is tangential
The bigger centrifugal force of the stronger tangential velocity of speed is more easy to get rid of solid particle to wall, now, in the presence of gravity and centrifugal force,
It is easy to separate solid particle entrained in effective synthesis gas and synthesis gas.In addition, when guide 2225 is led to be square
When to block, guiding gutter can be set to obtain relatively narrower, can stop that bulky grain dust enters in central tube 2223 or from center
Flowed out in pipe 2223；Further improve dust removing effects.And guiding gutter is set to be passed through from the side of remote central tube 2223 of square guide pad
Wear to close to the side of central tube 2223, then provided convenience for the outflow of synthesis gas.
Square guide pad tilts to close to the direction of the first dust discharging port 2222, so, not only with certain inertial dust collection
Effect due in movement air flow grit and gas there are different inertia force, dusty gas zig zag or with certain barrier
During collision, the movement locus of grit will be separated, and cause synthesis gas under the guide effect of long and narrow guide channel 22251
Formed with certain orientation and the stronger air-flow of directionality, these leave the direction of the air-flow of respective guide channel 22251 all with
Central tube circumference is tangent, and so these air-flows for leaving respective guide channel 22251 accumulate the gas of one corkscrew motion again
Stream, and this strand of bigger centrifugal force of the stronger tangential velocity of spiral air flow tangential velocity formed under this spline structure is more easy to solid particle
Get rid of to wall, so, in the presence of gravity and centrifugal force, be easy to solid entrained in effective synthesis gas and synthesis gas
Particle separates.Furthermore, it is possible to which guiding gutter is set to obtain into relatively narrower, it can stop that bulky grain dust enters in central tube 2223 and flow
Go out, further improve dust removing effects.
Preferably, the body below cone of central tube 2223 further prevents from closing than thin above cone
Flowed out into gas from the second dust discharging port 2224.
Further illustrate that the course of work of the cyclone dust collectors of the present invention is as follows：
Synthesis gas flows into central tube 2223 from top to bottom from cooling chamber 2212, lime-ash also with synthesis gas from top to bottom down
Falling, and guide 2225 is sets diagonally downward, synthesis gas motion of being spinned when being come out from guide 2225 is separated, due to
Block on the top of guide 2225 so that little particle preferably settles and is not easy to be blown afloat, so as to obtain the good of smaller particle
Separating effect.The bottom of central tube 2223 is provided with cone 2226, the lime-ash that can effectively prevent from falling is due to the stream of air-flow
Move and blown afloat raising dust removing effects, additionally it is possible to avoid a part of synthesis gas from being directly entered dust discharging port.First cyclone dust collectors 222
It can will enter the synthesis gas inside dedusting chamber 2227 and central tube 2223 and the solid particle of synthesis gas carrying well
Separate, additionally it is possible to prevent that the solid particle in central tube 2223 from disturbing and/or a large amount of synthesis gas flow from the second dust discharging port 2224
Go out, substantially increase the dust removing effects of cyclone dust collectors and enterprise obtains the amount of smart synthesis gas, realized using simple structure
Multistage dedusting, the present invention in level Four dedusting, i.e.,：The first order, upper half chamber, by screw, centrifugal force and gravitational dust collection；Second
Level, lower half chamber, by screw, centrifugal force and gravitational dust collection；The third level, the inertial dust collection of guide；The fourth stage, center
Pipe, by screw, centrifugal force and gravitational dust collection.
In the present embodiment, the first cyclone dust collectors 222 are arranged at the syngas outlet 2214 of cooler 221, and the
The import of one cyclone dust collectors 222 connects with the syngas outlet 2214 of cooler 221, the outlet of the first cyclone dust collectors 222
Form the gas outlet of cooling device 22.During connection, by the central tube 2223 and cooler of the first cyclone dust collectors 222
221 syngas outlet 2214 connects.
In the present embodiment, the air inlet 2113 of heat exchanger 21 is connected with the first gas outlet 119 of coal gasifier 11, cooling
The air inlet of device 22 is connected with the gas outlet 2112 of heat exchanger 21, and heat exchanger 21 is respectively provided with heat exchanger tube with cooling device 22,
The heat exchanger tube of heat exchanger 21 in the heat exchanger tube of cooling device 22 with being connected with cooling medium, and the cooling medium is to flowing through heat exchanger 21
The heat carried with the synthesis gas of cooling device 22 is reclaimed.In the present embodiment, water-coal-slurry through the burning of coal gasifier 11 at
After reason, generate with CO and H2Based on, temperature 1350 degrees centigrades synthesis gas, the synthesis gas generation carry big calorimetric
Amount, when synthesis gas flows through heat exchanger 21 and cooling device 22, carries out heat exchange between cooling medium and synthesis gas so that close
Absorbed into the energy entrained by gas by the cooling medium in the heat exchanger tube of heat exchanger 21 and cooling device 22, to coal water slurry gasification work
The heat energy of synthesis gas in process system is reclaimed again.
(3) second cyclone dust collectors 60
Referring to shown in Fig. 7 to Fig. 9, heat recovery unit 20 also includes the second cyclone dust collectors 60, second cyclone dust removal
Device 60 is connected on the pipeline between the gas outlet of heat exchanger 21 and the air inlet of cooling device 22, removes what is carried in synthesis gas
Lime-ash, the structure of the second cyclone dust collectors 60 and the structure complete one of the first cyclone dust collectors 222 in the present embodiment are to different
, the inlet and outlet direction of the synthesis gas in systems of the second cyclone dust collectors 60 is opposite.Now, the second whirlwind removes
The entrance of dirt device 60 is through hole 2228, the upper port of pipe 2223 centered on outlet, and specific connected mode is shown in Figure 1.Synthesis
Gas is connected from through hole 2228 with the tangential direction of upper half chamber 22271 of the second cyclone dust collectors 60, and the crude synthesis gas containing lime-ash is from upper
The through hole 2228 of half chamber 22271 enters rear screw and moved, and the reliable gravity of bulky grain and centrifugal force separate in upper half chamber 22271,
Prevent the dust of bulky grain from wearing guide 2225；Synthesis gas is downwardly into lower half chamber 22272, while gas solid separation, closes
Enter into gas from the guiding gutter of guide 2225 inside central tube 2223, guide 2225 and central tube 2223 be it is tangentially connected,
Synthesis gas enters central tube 2223 after guide 2225 removes a part of solid particle by inertial dust collection, carries out spiral again
Motion, the reliable gravity of grey solid impurity particle and centrifugal force separate in central tube 2223；Guide 2225 and central tube 2223 are tangential
Connection, and the guiding gutter gap for the multiple guides 2225 being uniformly arranged is settable smaller so that carry the synthesis gas one of lime-ash secretly
Beginning just presses close to inwall and forms preferable screw, and under gravity and centrifugal action, its inertial dust collection acts in addition, relatively
Then there is more preferably separating effect in common cyclone separator；The bottom of central tube 2223 is provided with block piece, i.e. cone
2226, the lime-ash that effectively can prevent from falling is blown afloat herein due to flow perturbation.
4th, washing unit 30, it is connected with heat recovery unit 20, to the synthesis gas after being handled from heat recovery unit 20
Carrying out washing treatment is carried out, place mat is carried out for the later use of synthesis gas.The washing unit 30 includes scrubbing tower 31, the water being sequentially connected
Coal gas conveyer 32, water-gas filter 33 and water-gas separator 34.
(1) scrubbing tower 31
Shown in Figure 10, the scrubbing tower 31 includes the 3rd housing 310, down-comer 320 and spiral stream guidance blade 330,
Wherein, the 3rd housing 310, which encloses, sets to form washing cavities 311, and washing cavities 311 are built with cleaning solution；Down-comer 320 is from the 3rd housing
310 outside is extended in washing cavities 311, and the outlet side in washing cavities 311 of down-comer 320 is arranged on the liquid of cleaning solution
Below face；Spiral stream guidance blade 330 is arranged in the cleaning solution of washing cavities 311 around down-comer 320, is led to forming spiral stream guidance
Road 340, and the air outlet of down-comer 320 is less than spiral stream guidance blade 330.Using the present embodiment scrubbing tower when, synthesis gas
Enter from down-comer 320 in washing cavities 311, and washing is entered from the air outlet being arranged in cleaning solution of down-comer 320
In liquid, now, synthesis gas is risen in the form of bubble in cleaning solution to the direction of the liquid level of cleaning solution.Due to spiral stream guidance leaf
The guide functions of piece 330, liquid level of the bubble that synthesis gas is formed along the flow-guiding channel that spiral stream guidance blade 330 is formed to cleaning solution
Direction is moved, and adds run duration and distance of the bubble in cleaning solution, now, the dust that cleaning solution can carry to bubble
Longer time, more fully effectively washing, and then wash out more dusts are carried out, makes ash fall in the bottom of washing cavities 311,
At the same time, because the guide effect of spiral stream guidance passage 340, bubble can be stretched in strip, bubble and washing are added
The contact area of liquid, enhance clean result of the cleaning solution to synthesis gas.In addition, the process for motion of being spinned in synthesis gas bubble
In, due to centrifugal action, dust is got rid of to the internal face direction of washing cavities 311 in bubble, when dust is thrown to bubble and washing
The contact interface of liquid is just washed liquid and moistens and wash out, and so as to which effective synthesis gas and dust separation be opened, realizes to synthesis gas
Abundant washing, and further improve cleaning solution to the clean result of synthesis gas.
Preferably, washing cavities 311 are close in the outward flange of the remote down-comer 320 of spiral stream guidance blade 330 in the present embodiment
Internal face.When synthesis gas enters in cleaning solution from the air outlet of down-comer 320, the gas formed by synthesis gas is prevented
Steep from the gap outflow between the internal face of the outward flange of spiral stream guidance blade 330 and washing cavities 311, improve scrubbing tower to synthesis
The clean result of gas.It is fixed on it is highly preferred that spiral stream guidance blade 330 spirals on down-comer 320 so that all by synthesis gas shape
Into bubble can only all be flowed from spiral stream guidance passage 340 can to cleaning solution liquid level rise, further improve washing
Clean result of the tower to synthesis gas.
Referring again to shown in Figure 10, the washing cavities 311 in the present embodiment are cylindrical cavity, and it is straight that down-comer 320 includes first
The straight length 322 of pipeline section 321 and second, wherein the first straight length 321 is perpendicular to the 3rd housing 310 and outside the 3rd housing 310
Portion extends to the inside of washing cavities 311；Axis arrangement of second straight length 322 along cylindrical cavity, and the second straight length 322
Upper end and one end in washing cavities 311 of the first straight length 321 are connected, and the lower end of the second straight length 322 extends to washing
The bottom of chamber 311 so that cleaning solution can sufficiently be washed to the synthesis gas come out from down-comer 320.
Preferably, spiral stream guidance blade 330 spirals from the lower end of the second straight length 322 and extended at the liquid level of cleaning solution,
Run duration of the bubble in cleaning solution can be extended as much as possible, the synthesis gas in bubble can more fully be washed liquid and wash
Wash.
Preferably, the bottom of cylindrical cavity is in funnel-shaped structure, after the dust on surface in synthesis gas bubble is washed out, meeting
Deposit to the bottom of funnel-shaped structure, and its lowest position of funnel-shaped structure is provided with scum pipe 350, the scum pipe 350 from
The bottom of funnel-shaped structure extends to the outside of the 3rd housing 310, so as to which the lime-ash of the bottom of washing cavities 311 is discharged into washing cavities
311。
In the present embodiment, the first straight length 321, which is located at, is provided with venturi at the other end outside the 3rd housing 310 and washes
Device 360 is washed, the opening position of the close liquid level of scrubbing tower is provided with a leakage fluid dram, a Quench water pump is provided with leakage fluid dram.
During use, a part of cleaning solution of scrubbing tower is sent into Venturi scrubber 360 by Quench water pump, when synthesis gas is from venturi
When washer 360 is entered in down-comer 320, the process water that chilled water pumping comes can fill entrained solid particle in synthesis gas
Share in the benefit wet, when synthesis gas, which enters, washs strong, solid particle can be deposited in the bottom of washing cavities 311 in the presence of self gravitation
Portion, and then excreted out from scum pipe 350, Residue extraction pipeline can select continuous outer row or periodically intermittent according to actual conditions
Outer row.
Referring again to shown in Figure 10, the scrubbing tower of the present embodiment also includes the solid valve type column plate 370 of polylith, polylith Gu Fashita
Plate 370 is fixedly installed on the inwall of washing cavities 311 and consolidates valve type column plate 370 perpendicular to the axis of cylindrical cavity, polylith
Upper end is provided with condensate inlet, and when being passed through condensate liquid into condensate inlet, the synthesis gas of rising is along down-comer 320
Annular space is upward through the solid valve type column plate 370 of polylith, is inversely contacted with condensate liquid, the synthesis gas after being washed to scrubbed liquid enters
Row washs again.
The top of washing cavities 311 is provided with scrubbing tower syngas outlet 380, washing and solid valve type column plate by cleaning solution
After 370 washing, flowed out from the top of washing cavities 311.
Scrubbing tower also includes demister 390, and the demister 390 is fixedly installed in washing cavities 311, and positioned at the solid valve of polylith
Between formula column plate 370 and scrubbing tower syngas outlet 380, gas-liquid separation is carried out, the mist being entrained in synthesis gas is removed, avoids
From the synthesis gas that scrubbing tower syngas outlet 380 comes out from carrying substantial amounts of cleaning solution.
In the present embodiment, when scrubbing tower normal operation, the main body of spiral stream guidance blade 330 is all submerged in water, due to
The unique helical structure of the main body of spiral stream guidance blade 330 so that synthesis gas is after the outlet out of down-comer 320, along spiral
After guide vane 330 does a few screw upwards, water layer is just passed；Due to the unique spiral shell of the main body of spiral stream guidance blade 330
Structure is revolved, synthesis gas is mainly run with elongated strip bubble in cleaning solution, relative to synthesis gas in the prior art in scrubbing tower
The mode that big stock bubble rises in water-bath, the synthesis gas of screw will have bigger contact area with water, so, relative to existing
There is a technology, the longer contact area of the stroke of synthesis gas in a water bath bigger time of contact is longer in the present invention so that in synthesis gas
Solid particle elution is better；Most of solid particles sediment of synthesis gas separates to water-bath is interior with synthesis gas.
The air inlet of the scrubbing tower 31 of the present embodiment is connected with the gas outlet of cooling device 22 by the 7th pipeline 107, right
Synthesis gas after heat recovery is washed, and ceramic filter 70 is provided with the 7th pipeline 107, again separating synthetic gas
In little particle dust.
The entrance of water-gas conveyer 32 is connected with the outlet of scrubbing tower 31 by the 9th pipeline 108.Water-gas filter
33 entrance is connected with the outlet of water-gas conveyer 32 by the tenth pipeline 109.The entrance of water-gas separator 34 and water coal
The outlet of air filter 33 is connected by the 11st pipeline 110.
Synthesis gas after scrubbed tower 31 washs still carries a small amount of solid particle or even has and can be catalyzed conversion
The impurity and aqueous water of agent poisoning and deactivation, therefore water-gas filter 33 and water-gas are provided with after water-gas conveyer 32
Separator 34, further removes the solid particle and aqueous water that synthesis gas carries, and synthesis gas passes through water-gas filter 33 and water
Just enter downstream transforms device after coal gas separator 34, so as to preferably protect the transformation catalyst in downstream, ensure downstream unit
Stable operation.
5th, partially synthetic gas reflux unit 50, each structure in heat recovery unit 20 is protected.
Coal-water slurry gasification system also includes partially synthetic gas reflux unit 50, and partially synthetic gas reflux unit 50 includes
8th pipeline 51 and compressor 52.The first end of wherein the 8th pipeline 51 is connected to the He of ceramic filter 70 of the 7th pipeline 107
On duct section between scrubbing tower 31, compressor 52 is arranged on the 8th pipeline 51, the second end of the 8th pipeline 51 and coal gasification
The low temperature synthesis gas entrance 117 of stove 11 connects；Compressor 52 is arranged on the 8th pipeline 51.The 7th pipeline is flow to through supercooling
107 synthesis gas it is very low, about 390 DEG C or so, now, the setting of the 8th pipeline 51 can be defeated by the synthesis of low temperature
Deliver in the tedge 116 of coal gasifier 11, with just from combustion chamber outflow synthesis gas be sufficiently mixed after, can reduce from
Gas burner outflow synthesis gas temperature, avoid the temperature of synthesis gas too high and damage the heat exchanger 21 in the downstream of coal gasifier 11,
The follow up device such as the second cyclone dust collectors 60, cooling device 22 and scrubbing tower 31.The setting of compressor 52 can be by after cooling
Synthesis gas be compressed, be easy to the synthesis gas of low temperature being delivered to coal gasifier 11.
6th, usage on black water unit 40, it is connected with washing unit 30, the Heisui River left after washing synthesis gas is handled,
Avoid polluting environment.
The Heisui River of coal gasifier 11 and scrubbing tower 31 is flashed by level Four, parses sour gas, and the Heisui River of slag bath passes through two
Level vacuum flashing, flashes off toxic and harmful gas.Flash system is divided into high pressure flash, low pressure flash, the first vacuum flashing and
Two vacuum flashings.
Shown in Figure 1, hp flash drum 43 is passed through in the Heisui River that coal gasifier 11 and scrubbing tower 31 flow out successively, and low pressure is dodged
The flash distillation process of steaming pot 44 and vacuum flasher 45, the processing procedure are consistent with existing Texaco Coal Gasification Process.Flash distillation
After processing, Heisui River, which enters in subsider 41, to be settled.
The usage on black water unit 40 of the present embodiment has grinding pond 42, grinds in pond 42 and is provided with grinding pond pump
47, grind and connected between pond pump 47 and subsider 41 by the 12nd pipeline 100, and control is provided with the 12nd pipeline 100
Valve 200 processed.In the prior art, the buck for grinding pond 42 returns to subsider 41 and the shared pipeline of slag bath pump discharge, mutually
Interference, influences to pump, and make the water quality of gasification ash water by large effect.Individually pond pump 47 is ground in laying in the present invention
To the 12nd pipeline 100 of subsider 41, so, the slag bath water and go the grinding water of subsider 41 not do mutually that slag pool pump is got
Disturb, help to improve the operation conditions of ash water system.And the inlet/outlet pipeline inner wall overlaying antifriction alloy of subsider underflow pump 49
Or lining ceramic lined, ensure system long period, oepration at full load.
In the course of work, settled from the Heisui River that vacuum flasher 45 flows out in subsider 41, the bottom of subsider 41
The higher mud of solid content, and deliver to vacuum filter from subsider 41 and carry out filtering means dehydration, filter cake is formed, and filter cake is sent out
Battery limit (BL)；The cake moisture that vacuum filter filters out is at least more than 50%, and this part is after vacuum filter absorbs water
Lime-ash filter cake sends processing outside after dehydration is further dried into cinder drier 46.The primary water overflow on the upper strata of subsider 41
To ash water tank 48, recycling.
In order to accelerate sinking speed of the Heisui River in subsider 41, flocculant is added in subsider 41.Subsider 41 is heavy
The fine ash (Gu the higher mud of amount or Heisui River also can) to lower is sent to vacuum band-type filter machine by subsider underflow pump 49
410.The primary water on the top of subsider 41 overflows to ash water tank 48 and recycled.
According to an embodiment of the invention, there is provided a kind of urgent interlock shutdown method of coal-water slurry gasification system, this
The coal-water slurry gasification system of embodiment is above-mentioned coal-water slurry gasification system.In the present embodiment, coal water slurry gasification
The urgent interlock shutdown method of process system includes：Absolute value and coal gasifier 11 when the rate of temperature change of coal gasifier 11
The absolute value of the rate of temperature change of the oxygen channel of connection and from scrubbing tower 31 flow out synthesis gas rate of temperature change it is exhausted
When being above the first preset value to value, make coal-water slurry gasification system shutdown；And/or the pressure change rate when coal gasifier 11
Absolute value, the absolute value of pressure change rate and the pressure change rate of the synthesis gas flowed out from scrubbing tower 31 of oxygen channel
When absolute value is above the second preset value, make coal-water slurry gasification system shutdown；And/or when abnormal conditions occur for compressor 52
When, make coal-water slurry gasification system shutdown；And/or in the oxygen channel being connected with coal gasifier 11, when center oxygen hose
When abnormal conditions occur for the oxygen gas flow rate in road, make coal-water slurry gasification system shutdown.It should be noted that here and coal
The oxygen channel that gasification furnace 11 connects is above-mentioned the first branch flow pipe 301a and the second branch flow pipe 302a, center oxygen pipeline
For the first branch flow pipe 301a.According to the method for the present embodiment, easily there is accident with reference in coal-water slurry gasification system
Or the position for accident occur must be prevented, i.e. coal gasifier 11, oxygen channel, compressor 52 and from scrubbing tower 31, with reference to temperature
Degree rate of change, pressure change rate and there is the conditions of abnormal conditions to realize that the urgent interlocking of coal-water slurry gasification system stops
The condition of car, emergency shut-down control device can be carried out to coal-water slurry gasification system exactly, ensure coal-water slurry gasification system
The operation stability of system, the generation of accident is avoided, whole system can be accurately controlled, ensure the person of operating personnel
Safety.During real work, as long as coal-water slurry gasification system meets any of the above conditions, coal-water slurry gasification system
Control centre's (not shown) with regard to control system perform shut-down operation.
In actual production process, relative to other positions, coal gasifier 11 and the oxygen feeding being connected with charging aperture 113
It is more that the quick-fried frequency of sudden strain of a muscle occurs for pipeline, i.e. the first branch flow pipe 301a and the second branch flow pipe 302a；And there is also oxygen pressure significantly
Fluctuation and the burner oxygen pipeline valve of coal gasifier 11 are the first regulating valve 36a, the second regulating valve 38a and the first check (non-return) valve
The hidden danger of leakage in 37a and the second check (non-return) valve 39a damages, now synthesis gas will be played a reversed role into oxygen feeding moment in coal gasifier 11
Pipeline, it will make the oxygen pipeline near charging aperture 113 that detonation occur first, it is at this moment, high low with the high height of pressure relative to temperature
Interlock shutdown, rate of temperature change and pressure change rate will be the important parameters that can faster react accident, when detonation occurs, temperature
Rise and the process of pressure change, although this time is very short, temperature and pressure, which reaches interlocking value, needs the time, and
Within this of short duration time, detonation spreads to more oxygen pipelines by what is be exceedingly fast, causes bigger security incident, deflagration
Middle temperature and pressure change are exceedingly fast greatly, and by computer system, temperature and pressure rate of change can obtain in the very short time
Go out, therefore rate of temperature change interlock shutdown is set in the present embodiment, it is rapid to cut off each valve of oxygen pipeline and establish elevated pressure nitrogen envelope, can have
Effect prevents the sprawling of detonation and the expansion of accident faster.Because one kind in the urgent interlock shutdown method of the present embodiment is basis
Rate of temperature change, in order that the temperature of system undying can not rise, avoids temperature too high and causes system come what is controlled
Blast.Therefore, in the present embodiment, when the temperature of coal gasifier 11 is higher than higher than the temperature of the 3rd preset value or oxygen channel
When the temperature of 4th preset value or the synthesis gas flowed out from scrubbing tower 31 is higher than five preset values, make coal-water slurry gasification system
Parking, reduce that system temperature is too high and the potential safety hazard brought.The 3rd preset value, the 4th preset value in the present embodiment and
Five preset values can determine that meeting is different with the change of each structure in coal-water slurry gasification system according to experiment, with
Exemplified by 5.5MPa coal gasifier 11, when coal gasifier 11 is more than 1800 DEG C or oxygen channel temperature be higher than 260 DEG C when,
Or from scrubbing tower 31 flow out synthesis gas temperature be higher than 280 DEG C when, be both needed to make system realize urgent interlock shutdown.
Preferably, in order to ensure the safety and stability of whole system, the first preset value in the present embodiment is 0.4
DEG C/ms to 0.6 DEG C/ms within the scope of, such as 0.3 DEG C/ms, it is highly preferred that the second preset value is in 9kpa/ms to 11kpa/ms
In the range of, such as 10kpa/ms, avoid the temperature change in system and pressure change it is too fast and cause system occur dodging it is quick-fried existing
As.
Similarly, relative to the high interlock shutdown low with pressure height of temperature, pressure change rate will can faster react thing
Therefore important parameter, when detonation occurs, temperature rise and pressure change process, although this time is very short, temperature
Reaching interlocking value with pressure needs the time, and within this of short duration time, detonation spreads to more oxygen by what is be exceedingly fast
Pipeline, causes bigger security incident, and temperature and pressure change are exceedingly fast greatly in deflagration, pass through computer system, temperature
It can be drawn in the very short time with pressure change rate, therefore pressure change rate interlock shutdown is set, cut off oxygen pipeline rapidly
Each valve seals with elevated pressure nitrogen is established, and can effectively prevent the sprawling of detonation and the expansion of accident faster.Because the present embodiment promptly joins
Lock parking method in it is a kind of controlled according to pressure change rate, the pressure of system undying can not rise, in order to
Avoid hypertonia and cause system to be exploded.Therefore, in the present embodiment, when the pressure of coal gasifier 11 is higher than the 6th preset value
Or the pressure of oxygen channel is higher than the 7th preset value or when the pressure of synthesis gas that is flowed out from scrubbing tower 31 is higher than eight preset values,
It is required to make coal-water slurry gasification system shutdown.The 6th preset value, the 7th preset value and the 8th in the present embodiment is default
Value determines that meeting is different with the change of each structure in coal-water slurry gasification system, with 6.5MPa coal gasification according to experiment
Exemplified by stove 11, when coal gasifier 11 is more than 6.75MPa or when the temperature of oxygen channel is higher than 6.75MPa or from scrubbing tower 31
When the temperature of the synthesis gas of outflow is higher than 6.75MPa, it is both needed to make system realize urgent interlock shutdown.
Because in the technique of the present invention, the synthesis gas (about 390 DEG C or so) after supercooling leaves ceramic filter
Some is returned to after being pressurized by compressor 52 after 70 enters the tedge 116 of coal gasifier 11 coal gasifier 11 is given birth to
Into (about 1300 DEG C or so) of high-temperature synthesis gas progress Quench, be allowed to high-temperature synthesis gas temperature and be down to 930 DEG C or so, if compression
Machine 52 abends operation, and 1300 DEG C or so of high-temperature synthesis gas of no Quench is directly entered the rotation of heat exchanger 21, second
The follow up device such as wind deduster 60, cooling device 22 and scrubbing tower 31, it will to equipment and normal damaging property of production
Influence so as to cause the generation of security incident, therefore need to set the interlocking of the exception parking of compressor 52 in the present embodiment.Compressor 52
Abnormal conditions include：The outlet pressure of compressor 52 is more than the 9th preset value；And/or outlet and the coal gasifier 11 of compressor 52
Between pressure difference absolute value higher than the tenth preset value or less than the 11st preset value；And/or the pressure change rate of compressor 52
Absolute value be more than the 12nd preset value.The 9th preset value, the tenth preset value, the 11st preset value in the present embodiment and
12 preset values determine all in accordance with experiment, and by taking 6.5MPa coal gasifier 11 as an example, the 9th preset value is 7.2 ± 0.5MPa, the
Ten preset values are 1.5 ± 0.5MPa, the 11st preset value is 0.5MPa and the 12nd preset value is 2kpa/ms.
Preferably, the 12nd preset value is in the range of 1.8kpa/ms to 2.2kpa/ms, such as 2.0kpa/ms.
Because in the oxygen channel that is connected with coal gasifier 11, center oxygen channel, i.e. the first direct current pipeline 301a more hold
Explosion accident easily occurs, therefore, it is also desirable to individually the working condition at the oxygen channel of center is individually monitored, i.e., it is central
When abnormal conditions occur for heart oxygen channel, it is also necessary to make coal-water slurry gasification system shutdown.Specifically, center oxygen hose
Road, i.e., abnormal conditions, which occur, for the oxygen gas flow rate in the first branch flow pipe 301a includes：Oxygen gas flow rate is more than the 13rd preset value, and
Three preset values may be set to 130% of normal flow when at full capacity, full so that 6.5Mpa coal feeding amounts are 1500 tons of gasification furnace as an example
Normally total oxygen gas flow rate is 42400Nm during load3/ h or so, central oxygen flow velocity be oxygen in the first branch flow pipe 301a just
Permanent current speed is in 6600Nm3/ h or so, now the oxygen gas flow rate in the first branch flow pipe 301a is more than 6600Nm3The 30% of/h is
8580Nm3/ h or so just makes the system shutdown.
In the running of coal gasifier 11, coal gasifier 11, the oxygen channel being connected with coal gasifier 11 and from washing
Washing the instantaneous pressure i.e. real-time pressure of the synthesis gas of the outflow of tower 31 can be measured by pressure sensor (or pressure gauge), pressure sensing
The real-time pressure signal or pressure data that device measures are sent to control centre, and control centre synchronously calculates the rate of change of pressure,
The curve that control centre can make pressure and change with time according to transmitting real-time pressure data, the slope of a curve
It is exactly pressure change rate.
In the running of coal gasifier 11, coal gasifier 11, the oxygen channel being connected with coal gasifier 11 and from washing
The transient temperature i.e. real time temperature for washing the synthesis gas of the outflow of tower 31 can have temperature sensor (or thermometer) to measure, TEMP
The real time temperature signal or temperature data that device measures are sent to control centre, and control centre calculates the rate of change of temperature, control
The curve that center can make temperature and change with time according to transmitting real-time temperature data, the slope of a curve are exactly
Rate of temperature change.
Similarly, pressure, temperature change and the pressure difference between coal gasifier 11 that compressor 52 exports can also lead to
Control centre's processing is delivered to after over-pressed force snesor and temperature sensor detection, and then monitors whole coal water slurry gasification work in real time
The running situation of process system, make system shutdown when exception occurs for compressor 52.
The urgent interlock shutdown method of the coal-water slurry gasification system of the present invention can effectively avoid the conjunction in coal gasifier
Carry pulverized coal particle into gas and play a reversed role to be formed into oxygen pipeline and dodge quick-fried potential safety hazard, enabling the holding of charging aperture longer time, its is excellent
Benign energy.The present invention, which is combined in coal-water slurry gasification system, easily there is the structure of accident, i.e. coal gasifier, oxygen hose
, combination temperature rate of change, pressure change rate and there is the conditions of abnormal conditions to realize water in road, compressor and from scrubbing tower
The condition of the urgent interlock shutdown of coal slurry gasification process system, coal-water slurry gasification system promptly can be stopped exactly
Car controls, and ensures the operation stability of coal-water slurry gasification system, avoids the generation of accident, can carry out essence to whole system
True control, ensure the personal safety of operating personnel.During real work, if coal-water slurry gasification system meet it is any of the above described
One condition, the control centre of coal-water slurry gasification system perform shut-down operation with regard to control system.
The preferred embodiments of the present invention are the foregoing is only, are not intended to limit the invention, for the skill of this area
For art personnel, the present invention can have various modifications and variations.Within the spirit and principles of the invention, that is made any repaiies
Change, equivalent substitution, improvement etc., should be included in the scope of the protection.
Claims (7)
1. a kind of urgent interlock shutdown method of coal-water slurry gasification system, it is characterised in that coal-water slurry gasification system
Including：Feed unit, gasification unit (10) and heat recovery unit (20), gasification unit (10) include coal gasifier (11)；Heat
Amount recovery unit (20) includes heat exchanger (21) and cooling device (22), wherein, the air inlet (2113) of the heat exchanger (21)
It is connected with the first gas outlet (119) of coal gasifier (11), the air inlet of cooling device (22) and going out for the heat exchanger (21)
Gas port (2112) connects, and the heat exchanger (21) is respectively provided with heat exchanger tube, the heat exchanger (21) with the cooling device (22)
Heat exchanger tube and the cooling device (22) heat exchanger tube in be connected with cooling medium, the cooling medium is to flowing through heat exchanger (21)
The heat carried with the synthesis gas of cooling device (22) is reclaimed, and the cooling device (22) includes：
Cooler (221), including cooling chamber (2212), synthesis gas entrance (2213) and syngas outlet (2214), the conjunction
The air inlet of the cooling device (22) is formed into gas entrance (2213)；
First cyclone dust collectors (222), it is arranged on syngas outlet (2214) place of the cooler (221), and described first
The import of cyclone dust collectors (222) connects with the syngas outlet (2214) of the cooler (221), first whirlwind
The gas outlet of cooling device (22) described in the export mixes of deduster (222)；
It is multiple to scrape slag cooling component (223), arranged along the length direction of the cooling chamber (2212), and each described scrape slag cooling group
Part (223) is respectively provided with heat exchanger tube；
The urgent interlock shutdown method of coal-water slurry gasification system includes：
Absolute value, the temperature for the oxygen channel being connected with the coal gasifier (11) when the rate of temperature change of coal gasifier (11)
It is default that the absolute value of the rate of temperature change of the absolute value of rate of change and the synthesis gas flowed out from scrubbing tower (31) is above first
During value, make coal-water slurry gasification system shutdown；And/or
The absolute value of the pressure change rate of absolute value, the oxygen channel when the pressure change rate of coal gasifier (11) and from
When the absolute value of the pressure change rate of the synthesis gas of scrubbing tower (31) outflow is above the second preset value, make the water-coal-slurry
Gasification process system shutdown；And/or
When abnormal conditions occur for compressor (52), make the coal-water slurry gasification system shutdown；And/or
In the oxygen channel, when abnormal conditions occur for the oxygen gas flow rate in the oxygen pipeline of center, make the water-coal-slurry gas
Chemical industry process system stops；
When coal gasifier (11) temperature higher than the 3rd preset value or the oxygen channel temperature higher than the 4th preset value or from
When the temperature of the synthesis gas of scrubbing tower (31) outflow is higher than five preset values, make coal-water slurry gasification system shutdown.
2. the urgent interlock shutdown method of coal-water slurry gasification system according to claim 1, it is characterised in that described
First preset value is within the scope of 0.4 DEG C/ms to 0.6 DEG C/ms.
3. the urgent interlock shutdown method of coal-water slurry gasification system according to claim 1, it is characterised in that work as coal
The pressure of gasification furnace (11) higher than the 6th preset value, the oxygen channel pressure higher than the 7th preset value and from the washing
When the pressure of the synthesis gas of tower (31) outflow is higher than eight preset values, make the coal-water slurry gasification system shutdown.
4. the urgent interlock shutdown method of coal-water slurry gasification system according to any one of claim 1 to 3, it is special
Sign is that the abnormal conditions of the compressor (52) include：
The outlet pressure of the compressor (52) is more than the 9th preset value；And/or
The absolute value of pressure difference between the outlet of the compressor (52) and the coal gasifier (11) higher than the tenth preset value or
Less than the 11st preset value；And/or
The absolute value of the pressure change rate of the compressor (52) is more than the 12nd preset value.
5. the urgent interlock shutdown method of coal-water slurry gasification system according to claim 1, it is characterised in that described
Abnormal conditions, which occur, for the oxygen gas flow rate in the oxygen channel of center includes：Oxygen gas flow rate in the oxygen channel is pre- more than the 13rd
If value.
6. the urgent interlock shutdown method of coal-water slurry gasification system according to claim 1, it is characterised in that described
Second preset value is in the range of 9kpa/ms to 11kpa/ms.
7. the urgent interlock shutdown method of coal-water slurry gasification system according to claim 4, it is characterised in that described
12nd preset value is in the range of 1.8kpa/ms to 2.2kpa/ms.
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| CN107216920B (en) * | 2016-03-22 | 2020-08-11 | 中国石油化工股份有限公司 | Safety control method of coal water slurry gasification furnace |
| CN106423160B (en) * | 2016-09-26 | 2018-08-28 | 中国科学院福建物质结构研究所 | The guard method of catalyst when coal-ethylene glycol dehydrogenation purification process stops in emergency |
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| CN110283630A (en) * | 2019-07-27 | 2019-09-27 | 河南心连心化学工业集团股份有限公司 | Coal chemical industry solid waste treatment device and treatment method |
| CN110643393B (en) * | 2019-10-21 | 2021-02-02 | 空气化工产品神华(上海)气化技术有限公司 | Multi-channel coal water slurry burner control system |
| CN112050091A (en) * | 2020-09-08 | 2020-12-08 | 上海氢枫能源技术有限公司 | Protection method for normal operation of hydrogenation machine |
| CN114907886A (en) * | 2021-02-08 | 2022-08-16 | 中国石油化工股份有限公司 | Central oxygen flow and valve position feedback control device and control method for coal water slurry gasification furnace |
| CN114907885A (en) * | 2021-02-08 | 2022-08-16 | 中国石油化工股份有限公司 | Central oxygen flow control device and control method for coal water slurry gasification furnace |
| CN115232651B (en) * | 2021-04-23 | 2024-03-29 | 中国石油化工股份有限公司 | Technological parameter monitoring and early warning method and device for coal gasification device |
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