CN104199413A - Emergency interlocking shutdown method for water-coal-slurry gasifying process system - Google Patents

Abstract

The invention provides an emergency interlocking shutdown method for a water-coal-slurry gasifying process system. The method is characterized in that shutdown is performed for the water-coal-slurry gasifying process system when the absolute value of temperature variation rate of a coal gasification furnace, the absolute value of the temperature variation rate of an oxygen pipeline which is connected with the coal gasification furnace, and the absolute value of the temperature variation rate of synthesis gas flowing from a washing tower are all higher than a first preset value, and/ or when the absolute value of the pressure variation rate of the coal gasification furnace, the absolute value of the pressure variation rate of the oxygen pipeline, and the absolute value of the pressure variation rate of the synthetic gas flowing from the washing tower are all higher than a second preset value, and/ or an abnormal condition occurs in a compressor, and/ or the flow rate of oxygen in a central oxygen pipeline suffers from abnormal condition. With the adoption of the emergency interlocking shutdown method, the water-coal-slurry gasifying process system can be accurately shut down and controlled in emergency, and therefore, the stability and safety of the water-coal-slurry gasifying process system in running can be ensured, and as a result, the accident is avoided.

Description

The urgent interlock shutdown method of coal water slurry gasification process system

Technical field

The present invention relates to coal water slurry gasification technology field, more specifically, relate to a kind of urgent interlock shutdown method of coal water slurry gasification process system.

Background technology

In normal production, the running status of coal water slurry gasification process system most of the time in High Temperature High Pressure, and its internal work medium is also and the material of inflammable, explosive, poisonous property, can say, safety in production and safe operation are extremely important for coal water slurry gasification process system, gasification furnace security system is exactly the safety interlock system for ensureing that gasified boiler system security of operation is set up, the interlocking that especially stops in emergency, the especially important leverage of safety.

In addition, in actual Chemical Manufacture, instrument sensing element there will be the situation of abnormal damage, and the data that at this moment instrument transmits are often understood distortion, and the interlock shutdown even leading to errors, causes unnecessary loss.The variate-value usually instrument sensing element senses being gone out in traditional method simply carries out 3 and selects 2 computing then to judge whether interlock shutdown, in the time that instrument sensing element there will be abnormal distortion, easily cause unnecessary interlock shutdown, cause unnecessary economic loss.

Visible, the interlocking that stops in emergency in existing Coal Gasification Technology is perfect not enough, can not ensure the safety movement of coal water slurry gasification process system.

Summary of the invention

The present invention aims to provide a kind of urgent interlock shutdown method of coal water slurry gasification process system, can not ensure to meet the problem of coal water slurry gasification process system safe operation to solve the urgent interlock shutdown method of coal water slurry gasification process system of the prior art.

For solving the problems of the technologies described above, according to an aspect of the present invention, a kind of urgent interlock shutdown method of coal water slurry gasification process system is provided, the urgent interlock shutdown method of this coal water slurry gasification process system comprises: when the absolute value of the rate of temperature change of the absolute value of the rate of temperature change of the absolute value of the rate of temperature change of coal gasifier, the oxygen channel that is connected with coal gasifier and the synthetic gas that flows out from scrubbing tower is during all higher than the first preset value, coal water slurry gasification process system is stopped; And/or when the absolute value of the pressure change rate of the absolute value of the pressure change rate of the absolute value of the pressure change rate of coal gasifier, oxygen channel and the synthetic gas that flows out from scrubbing tower is during all higher than the second preset value, coal water slurry gasification process system is stopped; And/or in the time of compressor generation abnormal conditions, coal water slurry gasification process system is stopped; And/or in oxygen channel, in the time of oxygen gas flow rate generation abnormal conditions in the oxygen pipeline of center, coal water slurry gasification process system is stopped.

Further, the temperature of the synthetic gas flowing out higher than the 4th preset value or from scrubbing tower higher than the temperature of the 3rd preset value or oxygen channel when the temperature of coal gasifier during higher than the 5th preset value, stops coal water slurry gasification process system.

Further, the first preset value is within the scope of 0.4 DEG C/ms to 0.6 DEG C/ms.

Further, the pressure of the synthetic gas flowing out higher than the 7th preset value and from scrubbing tower higher than the pressure of the 6th preset value, oxygen channel when the pressure of coal gasifier during higher than the 8th preset value, stops coal water slurry gasification process system.

Further, the abnormal conditions of compressor comprise: the top hole pressure of compressor is greater than the 9th preset value; And/or the absolute value of pressure reduction between outlet and the coal gasifier of compressor is higher than the tenth preset value or lower than the 11 preset value; And/or the absolute value of the pressure change rate of compressor is greater than the 12 preset value.

Further, the oxygen gas flow rate generation abnormal conditions in central oxygen feed channel comprise: the oxygen gas flow rate in oxygen channel exceedes the 13 preset value.

Further, the second preset value is in the scope of 9kpa/ms to 11kpa/ms.

Further, the 12 preset value is in the scope of 1.8kpa/ms to 2.2kpa/ms.

The technical scheme of application invention, the urgent interlock shutdown method of coal water slurry gasification process system maybe must stop to occur the position of accident in conjunction with the accident that easily occurs in coal water slurry gasification process system, it is coal gasifier, oxygen channel, compressor and from scrubbing tower, in conjunction with rate of temperature change, pressure change rate and occur that the condition of abnormal conditions realizes the condition of the urgent interlock shutdown of coal water slurry gasification process system, can carry out emergency shut-down control device to coal water slurry gasification process system exactly, ensure operation stability and the security of coal water slurry gasification process system, avoid the generation of accident, can control accurately whole system, ensure operating personnel's personal safety.When real work, as long as coal water slurry gasification process system meets above-mentioned any one condition, the control center of coal water slurry gasification process system carries out shut-down operation with regard to control system.

Brief description of the drawings

The accompanying drawing that forms the application's a part is used to provide a further understanding of the present invention, and schematic description and description of the present invention is used for explaining the present invention, does not form inappropriate limitation of the present invention.In the accompanying drawings:

Fig. 1 has schematically shown the front view of the coal water slurry gasification process system in the present invention;

Fig. 2 has schematically shown the front view of the coal gasifier in the present invention;

Fig. 3 has schematically shown heat interchanger of the present invention and has removed the vertical view after part shell;

The left view when doctor assemblies that Fig. 4 has schematically shown heat interchanger of the present invention is arranged on main shaft;

Fig. 5 has schematically shown the front view of the heat exchange unit of heat interchanger of the present invention;

Fig. 6 has schematically shown the front view of the cooling device in the present invention;

Fig. 7 has schematically shown the front view of the of the present invention first or second tornado dust collector;

Fig. 8 has schematically shown the A-A view of Fig. 7;

Fig. 9 has schematically shown the three-dimensional structure diagram of the guide in the present invention;

Figure 10 has schematically shown the front view of scrubbing tower of the present invention; And

Figure 11 has schematically shown the annexation figure of coal gasifier feed system of the present invention.

Description of reference numerals: 10, gasification unit; 11, coal gasifier; 111, firing chamber; 112, shock chamber; 113, charging aperture; 114, exhausr port; 115, through hole; 116, tedge; 117, low temperature synthetic gas entrance; 118, settler; 119, the first gas outlet; 120, slag-drip opening; 20, heat recovery unit; 21, heat interchanger; 211, the first housing; 2111, heat exchanging chamber; 2112, gas outlet; 2113, air intake opening; 212, heat exchange unit; 2121, heat-transfer surface; 2122, heat exchanger plates; 2123, heat exchanger tube; 2124, mounting hole; 213, doctor assemblies; 2131, scraper; 214, drive division; 2141, drive motor; 2142, main shaft; 215, seal; 22, cooling device; 221, refrigeratory; 2211, the second housing; 2212, cooling chamber; 2213, synthetic gas entrance; 2214, syngas outlet; 222, the first tornado dust collector; 223, scrape slag cooling package; 224, the first drum; 225, the second drum; 2221, shell; 2222, the first dust discharging port; 2223, pipe core; 2224, the second dust discharging port; 2225, guide; 22251, guide channel; 2226, cone; 2227, dedusting chamber; 22271, first chamber; 22272, second chamber; 2228, through hole; 2229, unload dirt gap; 224, the first drum; 225, the second drum; 30, washing unit; 31, scrubbing tower; 310, the 3rd housing; 311, washing cavities; 320, downtake; 321, the first straight length; 322, the second straight length; 330, spiral stream guidance blade; 340, spiral stream guidance passage; 350, scum pipe; 360, Venturi scrubber; 370, solid valve formula column plate; 380, scrubbing tower syngas outlet; 390, demister; 32, water gas conveyer; 33, water gas filtrator; 34, water gas separation vessel; 40, usage on black water unit; 41, subsider; 42, grind pond; 43, hp flash drum; 44, low pressure flash chamber; 45, vacuum flasher; 46, cinder exsiccator; 47, grind pond pump; 48, ash water tank; 49, subsider underflow pump; 410, band filter; 50, part synthetic gas reflux unit; 51, the 8th pipeline; 52, compressor; 60, the second tornado dust collector; 70, porcelain filter; 101, the first pipeline; 102, second pipe; 103, the 3rd pipeline; 104, the 4th pipeline; 105, the 5th pipeline; 106, the 6th pipeline; 107, the 7th pipeline; 108, the 9th pipeline; 109, the tenth pipeline; 110, the 11 pipeline; 100, the 12 pipeline; 200, operation valve; 10a, water-coal-slurry pipeline; 11a, the first operation valve; 20a, the first nitrogen pipeline; 21a, the second operation valve; 22a, the 3rd check (non-return) valve; 30a, oxygen channel; 301a, the first tributary pipeline; 302a, the second tributary pipeline; 31a, the 3rd operation valve; 32a, the 4th operation valve; 33a, the 5th operation valve; 34a, the 6th operation valve; 35a, the 4th pressure transducer; 36a, the first variable valve; 37a, the first check (non-return) valve; 38a, the second variable valve; 39a, the second check (non-return) valve; 40a, the second nitrogen pipeline; 401a, the first nitrogen tributary pipeline; 402a, the second nitrogen tributary pipeline; 403a, the 3rd nitrogen tributary pipeline; 404a, the 4th nitrogen tributary pipeline; 41a, the 4th check (non-return) valve; 42a, the 7th operation valve; 43a, the 5th check (non-return) valve; 44a, the 8th operation valve; 45a, the 6th check (non-return) valve; 46a, the 9th operation valve; 47a, the tenth operation valve; 48a, the 7th check (non-return) valve; 50a, the 3rd nitrogen pipeline; 51a, the 11 operation valve; 61a, the first pressure transducer; 62a, the second pressure transducer; 63a, the 3rd pressure transducer; 70a, burner; 81a, first arithmetic device; 82a, second arithmetic device.

Embodiment

Below in conjunction with accompanying drawing, embodiments of the invention are elaborated, but the multitude of different ways that the present invention can be defined by the claims and cover is implemented.

Referring to shown in Fig. 1 to Figure 11, the coal water slurry gasification process system in the present invention comprises: feed unit, gasification unit 10 and heat recovery unit 20.Gasification unit 10 comprises coal gasifier 11; Heat recovery unit 20 comprises heat interchanger 21 and cooling device 22, wherein, the air intake opening 2113 of heat interchanger 21 is connected with the first gas outlet 119 of coal gasifier 11, the air intake opening of cooling device 22 is connected with the gas outlet 2112 of heat interchanger 21, and heat interchanger 21 all has heat exchanger tube with cooling device 22, in the heat exchanger tube of the heat exchanger tube of heat interchanger 21 and cooling device 22, be all connected with heat eliminating medium, the heat that this heat eliminating medium carries the synthetic gas of flow through heat interchanger 21 and cooling device 22 reclaims.While using coal water slurry gasification process system of the present invention, after coal water mixture being passed in coal gasifier 11, coal water mixture is processed and is generated with CO and H through burning ₂be main synthetic gas, the now extreme temperatures of synthetic gas, 1350 degrees Celsius of left and right.When synthetic gas flow to heat interchanger 21 and cooling device 22 from coal gasifier 11, between the heat eliminating medium in the heat exchanger tube of the heat exchanger tube of heat interchanger 21 and cooling device 22 and synthetic gas, carry out heat interchange, thereby the heat in synthetic gas is reclaimed.

This coal water slurry gasification process system mainly comprises:

One, feed unit

Shown in Figure 1, the direction of arrow in figure represents the flow direction of ducted fluid.The coal gasifier feed unit of applying parking method of the present invention specifically comprises:

Water-coal-slurry pipeline 10a, this water-coal-slurry pipeline 10a is connected with the burner 70a of coal gasifier, is provided with the first operation valve 11a on water-coal-slurry pipeline 10a, and this first operation valve 11a controls the break-make of water-coal-slurry pipeline; The first nitrogen pipeline 20a, on this first nitrogen pipeline 20a, be provided with the second operation valve 21a and the 3rd check (non-return) valve 22a, wherein, the first nitrogen pipeline 20a is connected with water-coal-slurry pipeline 10a, link position is positioned on the duct section that the endpiece with the first operation valve 11a of water-coal-slurry pipeline 10a is connected, and the 3rd check (non-return) valve 22a is arranged on the duct section between link position and the second operation valve 21a of the first nitrogen pipeline 20a and water-coal-slurry pipeline 10a.In the time that the first operation valve 11a is closed, open the second operation valve 21a, in the first nitrogen pipeline 20a, pass into high pressure nitrogen, just the water-coal-slurry pipeline in water-coal-slurry pipeline 10a can be purged to coal gasifier, the setting of the 3rd check (non-return) valve 22a can avoid the fluid in water-coal-slurry pipeline 10a to be back in the first nitrogen pipeline 20a.

Coal gasifier feed system also comprises oxygen channel 30a, and this oxygen channel 30a comprises the first tributary pipeline 301a and the second tributary pipeline 302a, and the first tributary pipeline 301a is all connected with burner 70a with the second tributary pipeline 302a.To the pipeline of the shunting node of oxygen channel 30a, be disposed with the 3rd operation valve 31a, the 4th operation valve 32a, the 5th operation valve 33a from the charging aperture of oxygen channel 30a.On the first tributary pipeline 301a of oxygen channel 30a, once be provided with the 6th operation valve 34a, the first variable valve 36a and the first check (non-return) valve 37a along the flow direction of oxygen, and the 4th pressure transducer 35a that is also provided with the pressure size of the porch of detecting the first tributary pipeline 301a at the inlet end of the 6th operation valve 34a, the pressure that the aperture of the 6th operation valve 34a detects according to the 4th pressure transducer 35a is controlled.On the first tributary pipeline 301a, be also provided with for detection of the first check (non-return) valve 37a the second pressure transducer 62a to the pressure size of the pipeline between burner 70a, simultaneously, on burner 70a, be provided with the first pressure transducer 61a that detects the pressure size in coal gasifier, the first pressure transducer 61a is all connected with the first arithmetic device 81a of control system with the second pressure transducer 62a, and the result that first arithmetic device 81a detects the first pressure transducer 61a and the second pressure transducer 62a calculates to control the aperture of the first variable valve 36a.The second tributary pipeline 302a is upper is disposed with the second variable valve 38a and the second check (non-return) valve 39a along the flow direction of oxygen, the second check (non-return) valve 39a is provided with the 3rd pressure transducer 63a to the pipeline between burner 70a, and the result that the second arithmetic device 82a of control system detects the first pressure transducer 61a and the 3rd pressure transducer 63a calculates to control the aperture of the second variable valve 38a.

Coal gasifier feed system also comprises the second nitrogen pipeline 40a, the second nitrogen pipeline 40a comprises the first nitrogen tributary pipeline 401a, the second nitrogen tributary pipeline 402a, the 3rd nitrogen tributary pipeline 403a and the 4th nitrogen tributary pipeline 404a, and these four tributary pipelines are all connected with oxygen channel 30a, by the oxygen blow in oxygen channel 30a to coal gasifier.Wherein, the link position of the first nitrogen tributary pipeline 401a and oxygen channel 30a is on the pipeline between the 3rd operation valve 31a and the 4th operation valve 32a, and the first nitrogen tributary pipeline 401a is above disposed with the 7th operation valve 42a and the 4th check (non-return) valve 41a along the flow direction of nitrogen; The link position of the second nitrogen tributary pipeline 402a and oxygen channel is on the pipeline between the 4th operation valve 32a and the 5th operation valve 33a, and the second nitrogen tributary pipeline 402a is above disposed with the 8th operation valve 44a and the 5th check (non-return) valve 43a along the flow direction of nitrogen; The 3rd nitrogen tributary pipeline 403a is connected with the second tributary pipeline 302a, and the link position between them is positioned on the pipeline being connected with the entrance point of the second variable valve 38a, and the 3rd nitrogen tributary pipeline 403a is above disposed with the 9th operation valve 46a and the 6th check (non-return) valve 45a along the flow direction of nitrogen; The 4th nitrogen tributary pipeline 404a is connected with the first tributary pipeline 301a, and their connection position is on the pipeline between the 6th operation valve 34a and the first variable valve 36a, and the 4th nitrogen tributary pipeline 404a is above disposed with the tenth operation valve 47a and the 7th check (non-return) valve 48a along the flow direction of nitrogen.

Shown in Figure 2, according to embodiments of the invention, the utilization of coal gasifier feed system control method for stopping realizes on the basis of above-mentioned coal gasifier feed system, specifically comprises: step S1: stop passing into oxygen and coal water mixture to the burner of coal gasifier; Step S2: utilize nitrogen that the oxygen in oxygen channel is purged to coal gasifier by burner; Step S3: keep the purging state to oxygen channel, and utilize nitrogen that the coal water mixture in water-coal-slurry pipeline is purged to coal gasifier by burner, water-coal-slurry pipeline was purged after first schedule time, stop the purging to water-coal-slurry pipeline; Step S4: keep the purging state to oxygen channel, and make the pressure in oxygen channel be greater than the pressure in coal gasifier, oxygen channel was purged after second schedule time, stop the purging to oxygen channel; Step S5: coal gasifier is carried out to pressure release.According to embodiments of the invention, in whole docking process, because the pressure in oxygen channel 30a is greater than the pressure in gasification furnace, can effectively avoid synthetic gas in gasification furnace to carry pulverized coal particle plays a reversed role and forms and dodge quick-fried phenomenon in oxygen channel 30a, avoid too much coal ash to enter burner in the inner adhesion of burner simultaneously, make its premium properties of maintenance of burner energy longer time.It should be noted that, said nitrogen in the present embodiment, its pressure is greater than the pressure of the oxygen in oxygen channel 30a.In the present embodiment, the purging nitrogen in purging nitrogen and oxygen channel 30a in water-coal-slurry pipeline 10a is same source nitrogen, and pressure is equally high, is high pressure nitrogen, and generally we are called high pressure nitrogen by pressure higher than the nitrogen of 8.0MPa.

Illustrate the operating process of each step in conjunction with the coal gasifier feed system shown in Figure 11.Before parking, the first operation valve 11a, the 3rd operation valve 31a, the 4th operation valve 32a, the 5th operation valve 33a, the 6th operation valve 34a, the first variable valve 36a and the second variable valve 38a are all in open mode, and all the other operation valves are all in closed condition.

In step S1, close the first operation valve 11a, the 3rd operation valve 31a, stop the burner 70a of coal gasifier to pass into coal water mixture and oxygen, and then stop passing into coal water mixture and oxygen in coal gasifier.

Then carry out step S2, open the 7th operation valve 42a, the 8th operation valve 44a, the 9th operation valve 46a and the tenth operation valve 47a, and pass into high pressure nitrogen in the second nitrogen pipeline 40a, by the oxygen blow in oxygen channel 30a to coal gasifier.

Then carry out step S3, open the second operation valve 21a, in the first nitrogen pipeline 20a, pass into high pressure nitrogen, utilize high pressure nitrogen to purge water-coal-slurry pipeline 10a, coal water mixture in water-coal-slurry pipeline 10a is purged to coal gasifier, after keeping purging 12S, close the second operation valve 21a, now, coal water mixture in water-coal-slurry pipeline 10a is purged to coal gasifier completely, in other embodiments of the invention, can also adjust according to actual behaviour in service the purge time of water-coal-slurry pipeline 10a, but the purge time of oxygen channel 30a must be longer than the purge time of water-coal-slurry pipeline 10a.

Then carry out step S4, due in whole coal gasifier feed system, the position that potential safety hazard is the highest is positioned at the 3rd operation valve 31a to this section of oxygen channel of burner 70a, therefore as long as ensure that synthetic gas can not carry coal ash and play a reversed role to the security that can ensure whole system in the first tributary pipeline 301a and the second tributary pipeline 302a from coal gasifier.Therefore, in step S4, first make the pressure in the first tributary pipeline 301a be greater than the pressure in coal gasifier, ensure that the coal dust in coal gasifier can not played a reversed role to the first tributary pipeline 301a.

Preferably, in the present embodiment, on the first tributary pipeline 301a, be provided with the first check (non-return) valve 37a and the first variable valve 36a, the first variable valve 36a, the first check (non-return) valve 37a and the first variable valve 36a are along setting gradually away from the direction of burner 70a; On the first tributary pipeline 301a, be also provided with the second pressure transducer 62a, this second pressure transducer 62a for detection of the first check (non-return) valve 37a to the pressure in the duct section between burner 70a; On gasification furnace, be provided with the first pressure transducer 61a that detects the pressure in gasification furnace; In step S4, control system regulates the aperture of the first variable valve 36a automatically according to the magnitude relationship of force value of the first pressure transducer 61a and the second pressure transducer 62a detection and the pressure difference of setting, so that the first check (non-return) valve 37a is greater than the pressure in gasification furnace to the pressure in the duct section between burner 70a, avoid the coal dust in coal gasifier to play a reversed role to the first tributary pipeline 301a.

Preferably, control system comprises first arithmetic device 81a, this first arithmetic device 81a carries out computing to the force value of the first pressure transducer 61a and the second pressure transducer 62a detection, compare the first check (non-return) valve 37a to the pressure difference in pressure in the duct section between burner 70a and gasification furnace, and then the aperture of controlling the first variable valve 36a is greater than pressure in gasification furnace to ensure the first check (non-return) valve 37a to pressure in the duct section between burner 70a, avoid playing a reversed role of coal dust, improve the security of system.More preferably, in step S4, the first check (non-return) valve 37a to the pressure in the duct section between burner 70a and the pressure difference in gasification furnace in the scope of 0.01MPa to 0.03MPa, the first check (non-return) valve 37a to the pressure in the duct section between burner 70a than the high 0.01MPa to 0.03MPa of the pressure in coal gasifier.Avoid on the one hand coal dust in coal gasifier to play a reversed role and get back in oxygen channel, can also avoid on the other hand pressure difference excessive and produce potential safety hazard, in other embodiments of the invention, the value of pressure difference can also suitably change according to actual behaviour in service.

Coal gasifier feed system according to the present invention can be known, oxygen channel 30a comprises the second tributary pipeline 302a, the second tributary pipeline 302a is connected with burner 70a, in step S4, make the pressure in the second tributary pipeline 302a be greater than the pressure in coal gasifier, further improve the security of whole system.

Preferably, in the present embodiment, be provided with the second check (non-return) valve 39a and the second variable valve 38a on the second tributary pipeline 302a, the second check (non-return) valve 39a and the second variable valve 38a are along setting gradually away from the direction of burner 70a; On the second tributary pipeline 302a, be also provided with the 3rd pressure transducer 63a, the 3rd pressure transducer 63a for detection of the second variable valve 38a to the pressure in the duct section between burner 70a; In step S4, control system regulates the aperture of the second variable valve 38a automatically according to the magnitude relationship of force value of the first pressure transducer 61a and the 3rd pressure transducer 63a detection and the pressure difference of setting, so that the second check (non-return) valve 39a is greater than the pressure in coal gasifier to the pressure in the duct section between burner 70a, avoid the coal dust in coal gasifier to play a reversed role to the first tributary pipeline 301a, the security that further improves whole system.

Preferably, control system comprises second arithmetic device 82a, second arithmetic device 82a carries out computing to the force value of the first pressure transducer 61a and the 3rd pressure transducer 63a detection, compare the second check (non-return) valve 39a to the pressure difference in pressure in the duct section between burner 70a and coal gasifier, and then the aperture of controlling the second variable valve 38a is greater than pressure in coal gasifier to ensure the second check (non-return) valve 39a to pressure in the duct section between burner 70a, avoid playing a reversed role of coal dust, improve the security of system.More preferably, in step S4, the second check (non-return) valve 39a to the pressure difference in pressure in the duct section between burner 70a and gas Coalification furnace in the scope of 0.01MPa to 0.03MPa, the second check (non-return) valve 39a to the pressure in the duct section between burner 70a than the high 0.01MPa to 0.03MPa of the pressure in coal gasifier.Avoid on the one hand coal dust in coal gasifier to play a reversed role and get back in oxygen channel, can also avoid on the other hand pressure difference excessive and produce potential safety hazard, in other embodiments of the invention, the value of pressure difference can also suitably change according to actual behaviour in service.

After keeping the operation 15S of step S4, close the 4th operation valve 32a, the 7th operation valve 42a, the 8th operation valve 44a, stop the purge to oxygen channel 30a.

Then carry out step S5, burner 70a is carried out in pressure release operation pressure leak process, pressure release speed is less than 0.1MPa/min, avoids the too fast and inner parts structure in infringement coal gasifier of pressure release.Generally, when gasification furnace pressure is during lower than 0.4MPa, can be considered that pressure release finishes.After pressure release finishes, the 9th operation valve 46a and the tenth operation valve 47a close, and stop passing into high pressure nitrogen to oxygen channel 30a.First arithmetic device 81a and second arithmetic device 82a continue to come into operation, the first variable valve 36a and the second variable valve 38a continue respectively by the operation result of first arithmetic device 81a and second arithmetic device 82a, by control system control aperture with regulate first and second check (non-return) valve to the pressure difference in pressure in the duct section burner 70a and gas Coalification furnace in the scope of 0.01MPa to 0.03MPa.

After step S5, also comprise step S6: after pressure release finishes, keep the first check (non-return) valve 37a to be greater than the pressure in coal gasifier to the pressure in the duct section between burner 70a, and keep the second check (non-return) valve 39a to be greater than the pressure in coal gasifier to the pressure in the duct section between burner 70a, until oxygen channel 30a and water-coal-slurry pipeline 10a are removed from burner 70a.Keeping the pressure in oxygen channel between first and second check (non-return) valve and burner 70a is pressure-fired with respect to the pressure in coal gasifier, the furnace gas that prevents from gasifying carries that dust is played a reversed role or will in coal gasifier, be full of nitrogen, for using next time coal gasifier to carry out adequate preparation, avoiding drive next time is to occur dodging quick-fried phenomenon.Concrete operations are: after the 9th operation valve 46a and the tenth operation valve 47a close, open immediately the 11 operation valve 51a on the 3rd nitrogen pipeline 50a, switch to low-pressure nitrogen by high pressure nitrogen, continue to continue to pass into low-pressure nitrogen to oxygen channel, keep it to be full of nitrogen state, continue to keep the pressure in oxygen channel 30a to be greater than the pressure in coal gasifier, until oxygen channel 30a and water-coal-slurry pipeline 10a are removed from burner 70a.Water-coal-slurry pipeline 10a and oxygen channel 30a, after burner 70a splits out, after the flange port that oxygen channel is connected with burner is sealed, can close the 11 operation valve 51a and stop passing into nitrogen.In the present embodiment, said low-pressure nitrogen is the nitrogen that pressure is less than 0.8MPa, ensures that between first and second check (non-return) valve and burner 70a, the pressure in oxygen channel is slightly larger than the pressure in coal gasifier, prevents that the coal dust that synthetic gas carries in gasification furnace from playing a reversed role.

Two, gasification unit 10, mainly comprises coal gasifier 11.Utilize coal gasifier 11 to carry out gasification process to coal water mixture.

(1) coal gasifier 11

Shown in Fig. 1 and Fig. 2, coal gasifier 11 comprises body of heater, and this body of heater comprises firing chamber 111, shock chamber 112, charging aperture 113 and exhausr port 114, wherein, shock chamber 112 is arranged on the below of firing chamber 111, and the bottom of firing chamber 111 offers the through hole 115 being communicated with shock chamber 112; Charging aperture 113 is arranged on body of heater, and is communicated with firing chamber 111; Exhausr port 114 is arranged on the top of firing chamber 111, and is communicated with firing chamber 111.In the shock chamber 112 of whole coal gasifier 11, the inner parts structures such as downtake are not set, between firing chamber 111 and shock chamber 112, be to be directly communicated with, in the time that coal gasifier 11 is worked, coal water mixture and oxygen enter firing chamber 111 from charging aperture 113, after burning is processed, directly to drop into the water cooling of 112 bottoms, shock chamber by through hole 115 curing for remaining molten state lime-ash, because the bottom of shock chamber 112 is the water-bath with certain liquid level, because water-bath separates the slag-drip opening of shock chamber's 112 inner chambers and its bottom, so shock chamber's 112 inner chambers form an airtight chamber, now in firing chamber 111, interior burning produces by CO ₂, CO and H ₂the crude synthesis gas forming is discharged to 111 outsides, firing chamber from being arranged on the exhausr port 114 of 111 upper ends, firing chamber, and then realize the function that synthetic gas and lime-ash initial gross separation are opened, visible, adopt coal gasifier 11 of the present invention can realize coal gasifier 11 aerogenesis functions in the past, and do not need to arrange the internals such as downtake and chilling ring, cause the frequent phenomenon occurring of parking accident thereby avoided shock chamber's 112 internals to damage, improved coal gasifier 11 life cycles and stability.

Charging aperture 113 is positioned on firing chamber 111 with the position that is communicated with of firing chamber 111, and the position that approaches firing chamber 111 at charging aperture 113 arranges nozzle, in the present embodiment, nozzle is to link together with charging aperture is integrated in fact, and the oxygen that enters the high speed and high pressure that the coal water mixture of firing chamber 111 is injected into dispels and atomization.Preferably, charging aperture 113 in the present embodiment is even number, for example 4,6,8 etc., and this even number charging aperture 113 being circumferentially symmetrical arranged between two along firing chamber 111, now, the coal water mixture of two symmetrical nozzle ejections is clashed into fragmentation mutually, reaches the gasification efficiency of better atomizing effect and Geng Jia, and then has improved the gasification efficiency of coal water mixture in firing chamber 111.

Coal gasifier 11 also comprises the tedge 116 at the top that is arranged on body of heater, and this tedge 116 docks with exhausr port 114 and extends along the direction away from firing chamber 111.Because coal water mixture can produce lime-ash not of uniform size in the process of burning, under normal circumstances, most of lime-ash can sink and enter shock chamber 112 by through hole 115 and carry out coolingly, but a part of granular lime-ash can be followed crude synthesis gas, and (principal ingredient is CO ₂, CO and H ₂) discharge firing chamber 111.On exhausr port 114 to connecting after tedge 116, in crude synthesis gas the lime-ash of larger particles shape because of its density more greatly under Action of Gravity Field the interior ascending velocity of tedge 116 diminish gradually then stop rise, then oppositely slowly sink, again enter firing chamber 111, finally sink to shock chamber 112 and enter cooling curing in water-bath, thereby avoided too much lime-ash to enter together in the downstream unit of coal gasifier 11 with synthetic gas, Zong flow out coal gasifier 11 through the final slag-drip opening 120 of lime-ash of cooling curing.

Preferably, the body of heater in the present embodiment is column structure, and tedge 116 is straight tube, when ensureing synthetic gas circulation smoothness also for the backflow of lime-ash provides settlement space.And tedge 116, through hole 115 and the exhausr port 114 in the present embodiment all arranged along the central axis of column structure, further ensured the patency that synthetic gas and lime-ash are mobile.

Preferably, coal gasifier 11 also comprises settler 118, settler 118 is arranged on one end away from firing chamber 111 of tedge 116, and this settler 118 has cushion chamber, cushion chamber is communicated with tedge 116, the synthetic gas entering in cushion chamber from tedge 116 is carried out to buffered, the internal diameter of the cushion chamber of settler 118 is larger than the internal diameter of tedge 116, entering crude synthesis gas flow velocity slows down, the ability that makes crude synthesis gas carry solid particle dies down, and settles down thereby be more conducive to lime-ash in crude synthesis gas.Specifically, in tedge 116, gas-solid obtains initial gross separation, and when synthetic gas enters in large diameter settler 118, flow velocity declines rapidly, and the grey solid impurity particle of part also slows down thereupon and rises and then fall, further gas solid separation.

According to the present embodiment, when synthetic gas and lime-ash separated after, synthetic gas should be discharged to whole coal gasifier 11, therefore, on coal gasifier 11, be also provided with the first gas outlet 119, this first gas outlet 119 is arranged on one end away from tedge 116 of settler 118, and is communicated with cushion chamber, thereby the synthetic gas through after gas solid separation is discharged to coal gasifier 11.

Preferably, on the tedge 116 in the present embodiment and the inwall of cushion chamber, be provided with the inner liner of heat resistant and wear resistant, avoid settler 118 and tedge to be subject to particle and wash away, to improve the serviceable life of whole coal gasifier 11.

In the process of coal water slurry gasification, the downstream of coal gasifier 11 is provided with the setting such as Slag Scraping Device and fly-ash separator, and from the extreme temperatures of firing chamber 111 synthetic gas out, approximately 1300 degrees Celsius, and easily upstream device is caused to heat etching damage, therefore, on coal gasifier 11, be also provided with low temperature synthetic gas entrance 117, this low temperature synthetic gas entrance 117 is arranged on tedge 116 and with tedge 116 and is communicated with, while passing into low temperature synthetic gas from low temperature synthetic gas entrance 117, this low temperature synthetic gas can mix with the high-temperature synthesis gas of discharging from firing chamber 111, thereby reduce the temperature of the synthetic gas that enters coal compositor downstream.Now, can protect upstream device damaged by high temperature on the one hand, can also reduce on the other hand the economic input amount of the equipment in downstream, greatly save the cost of enterprise.

Three, heat recovery unit 20, is connected with gasification unit 10, and the synthetic gas forming after coal gasifier 11 is processed is processed, and reclaims the entrained heat of synthetic gas.This heat recovery unit 20 mainly comprises heat interchanger 21, cooling device 22 and the second tornado dust collector 60.The air intake opening 2113 of heat interchanger 21 is connected with the first gas outlet 119 of coal gasifier 11, the air intake opening of cooling device 22 is connected with the gas outlet 2112 of heat interchanger 21, and heat interchanger 21 all has heat exchanger tube with cooling device 22, in the heat exchanger tube of the heat exchanger tube of heat interchanger 21 and cooling device 22, be all connected with heat eliminating medium, the heat that this heat eliminating medium carries the synthetic gas of flow through heat interchanger 21 and cooling device 22 reclaims.

(1) heat interchanger 21

Shown in Fig. 1 Fig. 3 to Fig. 5, according to embodiments of the invention, heat interchanger 21 comprises: the first housing 211, heat exchange unit 212, doctor assemblies 213 and drive division 214, and wherein, the first housing 211 encloses and forms heat exchanging chamber 2111; Heat exchange unit 212 and doctor assemblies 213 are all arranged in heat exchanging chamber 2111; Drive division 214 drives doctor assemblies 213 to scrape the lime-ash on heat exchange unit 212.According to embodiments of the invention, under the driving of drive division 214, doctor assemblies 213 can scrape the lime-ash on heat exchange unit 212, avoids lime-ash to be deposited in heat exchanging chamber 2111 and causes the obstruction of heat interchanger, has effectively improved the heat transfer effect of heat interchanger.

Preferably, heat exchange unit 212 is multiple, can effectively improve the heat transfer effect of heat interchanger.In other embodiments, heat exchange unit 212 can be also one.According to the present embodiment, each heat exchange unit 212 includes heat-transfer surface 2121, doctor assemblies 213 is multiple, multiple doctor assemblies 213 arrange correspondingly with multiple heat-transfer surfaces 2121, under the driving of drive division 214, doctor assemblies 213 is moving near in the region of heat-transfer surface 2121, by the lime-ash scraping on heat-transfer surface 2121.

Preferably, multiple heat exchange units 212 side by side and interval arrange, and keep the heat-transfer surface 2121 of adjacent two heat exchange units 212 relative.Specifically, each heat exchange unit 212 includes two heat-transfer surfaces 2121, in the time that multiple heat exchange units 212 are spaced side by side, between two relative heat-transfer surfaces 2121, forms gap, and the fluid in the gap of flowing through is carried out to heat exchange processing.In the present embodiment, multiple heat exchange units 212 form many heat exchange gaps, after fluid enters heat interchanger, are divided into multiply and enter gap, have effectively improved the heat exchange efficiency of heat interchanger.

Preferably, drive division 214 comprises drive motor 2141, the main shaft 2142 of drive motor 2141 is through multiple heat exchange units 212, doctor assemblies 213 is fixedly installed on main shaft 2142, in the process of heat interchanger work, in the time that drive motor 2141 rotates, can drive the doctor assemblies 213 being arranged on main shaft 2142 to rotate on the one hand, thereby scrape the lime-ash on heat exchange unit 212, 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 the motion of lime-ash in space become more active, and then prevent the deposition of lime-ash.

In the present embodiment, doctor assemblies 213 comprises many scraper 2131, many scraper 2131 is circumferentially evenly arranged along the same of main shaft 2142, and multiple scrapers 2131 are all perpendicular to main shaft 2142, in the time that main shaft 2142 rotates, many scraper 2131 can, near moving in the region of heat-transfer surface 2121, be scraped to the lime-ash on heat-transfer surface 2121, and effectively improve the rate that scrapes of lime-ash.

Preferably, drive motor 2141 is arranged on the outside of the first housing 211, convenient operation and control.The middle part of each heat exchange unit 212 is provided with mounting hole 2124, the main shaft 2142 of drive motor 2141 stretches in heat exchanging chamber 2111 and runs through each mounting hole 2124, now, just can drive multiple doctor assemblies 213 with a drive motor 2141, greatly save the manufacturing cost of heat interchanger.More preferably, the contact position place of the main shaft 2142 of drive motor 2141 and the first housing 211 is provided with seal 215, prevents that main shaft 2142 from producing and revealing in the position contacting with the first housing 211.

Refer again to 3 and Fig. 5 shown in, heat exchange unit 212 also comprises polylith heat exchanger plates 2122 and heat exchanger tube 2123, polylith heat exchanger plates 2122 is enclosed to form rectangular parallelepiped installing space; Heat exchanger tube 2123 is arranged in installing space.According to the present embodiment, heat exchanger tube 2123 is arranged in the installing space that polylith heat exchanger plates 2122 is enclosed to form, and increases the heat interchanging area of heat exchange unit 212, improves the heat transfer effect of whole heat interchanger, and is convenient to install.More preferably, heat exchanger tube 2123 is wavy and is arranged in installing space, has increased the length of heat exchanger tube 2123, thereby has increased the heat eliminating medium in heat exchange unit 212, further improves the heat transfer effect of heat interchanger.In the present embodiment, the two ends of heat exchanger tube 2123 are stretched out heat transfer space and are arrived the outside of the first housing 211, are convenient to heat eliminating medium be sent into or got rid of the heat exchanging chamber 2111 of heat interchanger.

According to embodiments of the invention, on the first housing 211, be provided with synthetic gas gas outlet 2112 and air intake opening 2113, and gas outlet 2112 and air intake opening 2113 are oppositely arranged, make the lime-ash being scraped by doctor assemblies 213 can follow the fluid heat exchanging chamber 2111 of outflow heat exchanger together.Gas outlet 2112 can be not relative with air intake opening 2113 yet in other embodiments, as long as ensure that fluid and lime-ash in heat exchanging chamber 2111 can be excluded heat exchanging chamber 2111.

Preferably, heat-transfer surface 2121 is parallel to the axis of gas outlet 2112 and air intake opening 2113, also be that gap between adjacent two heat exchange units 212 is parallel to the line between gas outlet 2112 and air intake opening 2113, the lime-ash that further guarantee is scraped by doctor assemblies 213 can be followed the heat exchanging chamber 2111 of being discharged together heat interchanger by the fluid of heat exchange swimmingly, prevents that lime-ash is again deposited on the outside surface of heat exchange unit 212 in the time walking around heat exchange unit 212.

(2) cooling device 22, this cooling device 22 comprises refrigeratory 221, the first tornado dust collector 222 and multiple slag cooling package 223 of scraping.Refrigeratory 221 comprises cooling chamber 2212, synthetic gas entrance 2213 and syngas outlet 2214, and synthetic gas entrance 2213 forms the air intake opening of cooling device 22; The first tornado dust collector 222 are arranged on syngas outlet 2214 places of refrigeratory 221, and the import of the first tornado dust collector 222 is communicated with the syngas outlet 2214 of refrigeratory 221, the gas outlet of the export mixes cooling device 22 of the first tornado dust collector 222; Multiple slag cooling packages 223 of scraping arrange along the length direction of cooling chamber 2212, and respectively scrape slag cooling package 223 and all have heat exchanger tube.When work, synthetic gas enters from the air intake opening of cooling device 22, carries out coolingly in cooling chamber 2212, and carries out heat recovery by heat exchanger tube, then after the first tornado dust collector 222 dedustings from the outlet of the first tornado dust collector 222, i.e. cooling device 22 is got rid of in the outlet of cooling device 22.

Shown in Fig. 6, this cooling device comprises refrigeratory 221, this refrigeratory 221 comprises the second housing 2211, multiple slag cooling package 223 of scraping, wherein the second housing 2211 encloses and forms cooling chamber 2212, the top of cooling chamber 2212 is provided with synthetic gas entrance 2213, the bottom of cooling chamber 2212 is provided with syngas outlet 2214, and synthetic gas entrance 2213 forms the air intake opening of cooling device 22; Multiple slag cooling packages 223 of scraping are arranged along the length direction of cooling chamber 2212, high-temperature synthesis gas for cool stream in cooling chamber 2212 also reclaims the entrained heat of high-temperature synthesis gas, and multiple slag cooling package 223 of scraping is also for scraping the lime-ash in cooling chamber 2212.According to embodiments of the invention, in the time that synthetic gas enters cooling chamber 2212 from synthetic gas entrance 2213, that arranges along the length direction of cooling chamber 2212 scrapes slag cooling package 223 and can carry out synthetic gas on the one hand multistage cooling, its scraper can effectively scrape the lime-ash that is attached to heat exchanger surface on the other hand, scratches or puncture the bulk falling from cooling chamber 2212 slag that falls.The lime-ash scraping can flow into tornado dust collector from the synthetic outlet of cooling chamber 2212 bottoms with synthetic gas, removes the lime-ash in synthetic gas.Visible, cooling device of the present invention not only can improve the recovery of the heat to high-temperature synthesis gas, and is not easy the phenomenon that occurs that refrigeratory 221 is blocked, has greatly improved the cycle of device stable operation, has reduced cost and has improved benefit.

In the present embodiment, scrape the structure of slag cooling package 223 and the structure of heat interchanger 21 is basic identical, difference is, scrape slag cooling package 223 the first housing 211 is not set, but directly the heat exchange unit of heat interchanger 212, doctor assemblies 213 and drive division 214 are arranged on refrigeratory 221.Concrete installation site is shown in Figure 6.

The cooling device of the present embodiment also comprises the first drum 224 and the second drum 225, and wherein the first drum 224 and the second drum 225 are all arranged on the second housing 2211 outsides.Be three and (can require in cooling chamber, to arrange some according to concrete heat exchange and scrape slag heat interchanger and scrape slag cooling package 223, not necessarily three), three first and the 3rd that scrape in slag cooling package 223, also scrape slag cooling package 223 and scrape slag cooling package 223 near of syngas outlet 2214 near of synthetic gas entrance 2213 and be all connected with the first drum 224; The slag cooling package 223 of scraping that is positioned at centre position is connected with the second drum 225.

In the present embodiment, the slag cooling package 223 of scraping setting gradually along the length direction of cooling chamber 2212 carries out cooling to the synthetic gas in cooling chamber 2212 successively, carry out heat interchange, the heat eliminating medium that utilization is scraped in slag cooling package 223 absorbs the entrained heat of synthetic gas, in this process, the temperature of synthetic gas is successively decreased step by step, the first drum 224 can be become to the steam that temperature is different with the chilled water in the second drum 225, utilize these steam, can be used for driving arrangement and also can carry out secondary heat exchange, visible, the heat that the cooling device of the present embodiment can carry synthetic gas again reclaims and utilizes, greatly improve the efficiency of enterprise and avoided the loss of energy.

Specifically, in the first drum 224, chilled water is housed, scrape slag cooling package 223 near syngas outlet 2214, the entrance that is first heat exchanger tube of scraping slag cooling package 223 is connected with the first drum 224 by the first pipeline 101, and the first pipeline 101 first ends are arranged on the bottom of the first drum 224; Near syngas outlet 2214 scrape slag cooling package 223, i.e. the 3rd outlet of scraping the heat exchanger tube of slag cooling package 223 is connected with the first drum 224 by second pipe 102, second pipe 102 first ends are arranged on the top of the first drum 224; The entrance of scraping slag cooling package 223 near syngas outlet 2214 is connected with the first drum 224 by the 3rd pipeline 103, and the 3rd pipeline 103 first ends are arranged on the top of the first drum 224.In the course of the work, when carrying out when cooling the synthetic gas in cooling chamber 2212, chilled water in the first drum 224 flow near in each heat exchanger tube of scraping slag cooling package 223 of syngas outlet 2214 by the first pipeline 101, carry out heat interchange heat and produce steam with the synthetic gas in cooling chamber 2212, steam flows out from heat exchanger tube, and from flow to the top of the first drum 224 by second pipe 102, and be positioned at centre position scrape slag cooling package 223, second entrance of scraping the heat exchanger tube of slag cooling package 223 is connected with the second drum 225 by the 4th pipeline 104, the first end of the 4th pipeline 104 is arranged on the bottom of the second drum 225, the outlet that is positioned at the heat exchanger tube of scraping slag cooling package 223 in centre position is connected with the second drum 225 by the 5th pipeline 105, and the first end of the 5th pipeline 105 is arranged on the top of the second drum 225.Carrying out in the process of heat interchange, chilled water flows into the heat exchanger tube of scraping slag cooling package 223 in centre position from the 4th pipeline 104, in cooling chamber 2212, carry out after heat interchange forms steam flowing out from the 5th pipeline 105 with synthetic gas, and the entrance of the heat exchanger tube of heat interchanger 21 is connected with the second drum 225 by the 6th pipeline 106, and the first end of the 6th pipeline 106 is arranged on the top of the second drum 225.Now, steam in the second drum 225 more than liquid level can enter into the 6th pipeline 106, enter in the heat exchanger tube of heat interchanger 21, in heat exchanging chamber 2111, carry out after heat interchange flowing out from the endpiece of the heat exchanger tube of heat interchanger 21 with synthetic gas, just can obtain the overheated high pressure steam of high-quality.

In the present invention, cooling chamber 2212 vertically arranges, and the syngas outlet 2214 of its bottom is connected with the first tornado dust collector 222, is conducive to the gas solid separation operation of the fly-ash separator of bottom connection, thereby obtains better dust removing effects.

Cooling chamber 2212 inwalls are provided with Wear-resistant, high-temperature resistant and heat-insulating material, to prevent washing away and wearing and tearing of solid particle in synthetic gas, and the scattering and disappearing of synthetic gas heat; Because synthetic gas temperature is very high, scrape slag cooling package 223 and be arranged on cooling chamber 2212 inside, can effectively reduce heat loss and loss, cooling cavity structure is simple, and manufacturing cost is not high.In other embodiments of the invention, can be according to actual needs, two or more cooling chambers 2212 are set, when production, one comes into operation, and one as for subsequent use, like this can be in the situation that gasification furnace stop, the cooling chamber breaking down 2212 of operation is cut out to maintenance (for subsequent use comes into operation), increased the dirigibility of production operation, avoided the economic loss of stopping and causing.

The cooling device 22 of the present embodiment also comprises the first tornado dust collector 222, and these first tornado dust collector 222 are arranged on syngas outlet 2214 places of refrigeratory 221 bottoms, and the synthetic gas with lime-ash flowing out from compositor is carried out to dedusting.

Specifically, the first tornado dust collector 222 comprise shell 2221, pipe core 2223, guide 2225 and cone 2226, and wherein, shell 2221 encloses and forms dedusting chamber 2227, and the bottom in dedusting chamber 2227 is provided with the first dust discharging port 2222;

Pipe core 2223 is arranged in dedusting chamber 2227, the upper port of pipe core 2223 extends to the outside in dedusting chamber 2227, and upper port is connected with syngas outlet 2214, the synthetic gas of being convenient to after refrigeratory 221 enters tornado dust collector, the lower port of pipe core 2223 is the second dust discharging port 2224, the second dust discharging port 2224 extends to the first dust discharging port 2222, is rejected to the outside in dedusting chamber 2227 for getting rid of solid particle that pipe core 2223 deposits;

Guide 2225 is arranged in dedusting chamber 2227, and the medial extremity of guide 2225 is connected with pipe core 2223 is tangent, in the time that synthetic gas flows out from guide channel 22251, accumulate the air-flow of one corkscrew motion, like this, under the effect of gravity and centrifugal force, be convenient to solid particle entrained in effective synthetic gas and synthetic gas to separate, the outboard end of guide 2225 stretches out away from pipe core 2223, on guide 2225, have guide channel 22251, guide channel 22251 is communicated with pipe core 2223;

Cone 2226 is arranged in pipe core 2223, the installation site of cone in pipe core 2223 be the position that is communicated with pipe core 2223 lower than guide channel 22251, and the cone point of cone is arranged near being communicated with a side of position and being positioned on the axis of pipe core 2223 and flows out from the second dust discharging port 2224 for the solid particle disturbance and/or a large amount of synthetic gas that prevent pipe core 2223.

Between the inwall of the margin and center pipe 2223 of the bottom surface of cone 2226, form and unload dirt gap 2229, be convenient to the lime-ash in pipe core 2223 to get rid of.Cone 2226 be arranged on lower than guide channel 22251 and pipe core 2223 be communicated with position time, the solid particle at dust discharging port place and the synthetic gas flowing out from guide channel 22251 can be separated on the one hand, can also avoid on the other hand a large amount of synthetic gas to go out from dust discharging port.When synthetic gas from centered by manage 2223 upper port while entering, synthetic gas flows downward from the upper port of pipe core 2223, solid particle flows downward under the carrying secretly of synthetic gas thereupon, most of solid particle clashes into after cone 2226 or pipe core 2223 inwalls from unloading dirt gap 2229 landings (also playing the effect of inertial dust collection), and flow out from the second dust discharging port 2224, and synthetic gas chance cone 2226 flows out with spiral fashion from the guide channel 22251 of guide 2225 after stopping rear reversed flow.

Preferably, dedusting chamber 2227 comprises first chamber 22271 and second chamber 22272, is provided with through hole 2228 tangent with first chamber 22271 and that be communicated with on shell 2221, and the discharge of the synthetic gas in the first tornado dust collector 222 is convenient in the setting of through hole 2228.The bottom in second chamber 22272 in the present embodiment is funnel-shaped structure, and the first dust discharging port 2222 is positioned at its lowest position of funnel-shaped structure, manages 2223 the lower port near second chamber 22272 centered by the second dust discharging port 2224, is convenient to the discharge of solid particle.

Preferably, the volume in first chamber 22271 is less than the volume in second chamber 22272, and pipe core 2223 runs through first chamber 22271 and second chamber 22272, in this structure, in the time that synthetic gas is in first chamber 22271, flow velocity is fast, and the efficiency of dust collection to synthetic gas is provided, and in the time that synthetic gas enters in second chamber 22272, because cushion space is large, the flow velocity of synthetic gas slows down, and is convenient to the deposition of solid particle, has effectively improved dust removing effects.And guide 2225 is arranged in second chamber 22272, when synthetic gas flows out into second chamber 22272 from guide channel 22251, now, the synthetic gas flowing out can form helical flow in second chamber 22272 and first chamber 22271, under the effect of gravity and centrifugal force, after part solid particle is thrown to second chamber 22272 and first chamber 22271 inwalls, landing is got off, dedusting again, after dedusting, synthetic gas gas is discharged from through hole 2228, and solid particle is discharged from the first dust discharging port 2222 of second 22272 bottoms, chamber.Preferably, the bottom in second chamber 22272 is funnel-shaped structure, and the first dust discharging port 2222 is positioned at its lowest position of funnel-shaped structure, is convenient to the discharge of solid particle.

Preferably, guide 2225 is multiple, multiple guides 2225 are taken in synthetic gas while entering pipe core 2223 along the sustained height that is circumferentially evenly arranged and is positioned at pipe core 2223 of pipe core 2223, can form helical motion, are convenient to the solid particle in synthetic gas and gas to separate.

In the present embodiment, guide 2225 is square orienting lug, guide channel 22251 is for being arranged on the diversion trench on square orienting lug, and diversion trench caves in to top from the low side of square orienting lug, and is through to the side near pipe core 2223 from square orienting lug away from pipe core 2,223 1 sides.When guide 2225 is set to square orienting lug, can diversion trench be arranged narrowlyer, like this, not only there is the effect of certain inertial dust collection because grit in movement air flow and gas have different inertial force, when dusty gas takes a sudden turn or collides with certain barrier, the movement locus of grit will be separated, and make synthetic gas form and there is certain orientation and the stronger air-flow of directivity under long and narrow guide channel 22251 guide effects, these directions of leaving the air-flow of guide channel 22251 are separately all tangent with pipe core 2223 circumference, now, these leave the air-flow of guide channel 22251 separately and accumulate the air-flow of one corkscrew motion, and this strand of larger centrifugal force of the stronger tangential velocity of spiral air flow tangential velocity forming under this structure more easily gets rid of solid particle to wall, now, under the effect of gravity and centrifugal force, be convenient to solid particle entrained in effective synthetic gas and synthetic gas to separate.In addition, in the time that guide 2225 is square orienting lug, can diversion trench be arranged narrowlyer, can stop that bulky grain dust enters outflow in pipe core 2223 or from pipe core 2223; Further improve dust removing effects.And make diversion trench from square orienting lug be through to the side near pipe core 2223 away from pipe core 2,223 one sides, for the outflow of synthetic gas is provided convenience.

Square orienting lug tilts to the direction near the first dust discharging port 2222, like this, not only there is the effect of certain inertial dust collection because grit in movement air flow and gas have different inertial force, when dusty gas takes a sudden turn or collides with certain barrier, the movement locus of grit will be separated, and synthetic gas is formed under the guide effect of long and narrow guide channel 22251 there is certain orientation and the stronger air-flow of directivity, these directions of leaving the air-flow of guide channel 22251 are separately all tangent with pipe core circumference, these leave the air-flow of guide channel 22251 separately and accumulate the air-flow of one corkscrew motion like this, and this strand of larger centrifugal force of the stronger tangential velocity of spiral air flow tangential velocity forming under this spline structure more easily gets rid of solid particle to wall, like this, under the effect of gravity and centrifugal force, be convenient to solid particle entrained in effective synthetic gas and synthetic gas to separate.In addition, can diversion trench be arranged narrowlyer, can stop that bulky grain dust enters the interior outflow of pipe core 2223, further improves dust removing effects.

Preferably, the body that is positioned at cone below of pipe core 2223, than being positioned at the thin of cone top, further prevents that synthetic gas from flowing out from the second dust discharging port 2224.

The course of work that tornado dust collector of the present invention are described is further as follows:

Synthetic gas flows into pipe core 2223 from top to bottom from cooling chamber 2212, lime-ash is also with synthetic gas past whereabouts from top to bottom, and guide 2225 is for being tilted to lower setting, the synthetic gas motion of spinning out time from guide 2225 separates, due to blocking of guide 2225 tops, make the better sedimentation of granule and be difficult for being blown afloat, thereby obtaining more short grained good separating effect.Be provided with cone 2226 in the bottom of pipe core 2223, can effectively prevent that the lime-ash falling from being blown afloat raising dust removing effects due to flowing of air-flow, can also avoid a part of synthetic gas directly to enter dust discharging port.The first tornado dust collector 222 can be well separated entering the synthetic gas of dedusting chamber 2227 and pipe core 2223 inside and solid particle that synthetic gas carries, can also prevent that solid particle disturbance and/or a large amount of synthetic gas in pipe core 2223 from flowing out from the second dust discharging port 2224, greatly improve the amount that the dust removing effects of tornado dust collector and enterprise obtain smart synthetic gas, adopt simple structure to realize multistage dedusting, level Four dedusting in the present invention, that is: the first order, first chamber, rely on helical motion, centrifugal force and gravitational dust collection; The second level, second chamber, relies on helical motion, centrifugal force and gravitational dust collection; The third level, the inertial dust collection of guide; The fourth stage, pipe core, relies on helical motion, centrifugal force and gravitational dust collection.

In the present embodiment, the first tornado dust collector 222 are arranged on syngas outlet 2214 places of refrigeratory 221, and the import of the first tornado dust collector 222 is communicated with the syngas outlet 2214 of refrigeratory 221, the gas outlet of the export mixes cooling device 22 of the first tornado dust collector 222.In the process connecting, the pipe core of the first tornado dust collector 222 2223 is connected with the syngas outlet 2214 of refrigeratory 221.

In the present embodiment, the air intake opening 2113 of heat interchanger 21 is connected with the first gas outlet 119 of coal gasifier 11, the air intake opening of cooling device 22 is connected with the gas outlet 2112 of heat interchanger 21, and heat interchanger 21 all has heat exchanger tube with cooling device 22, in the heat exchanger tube of the heat exchanger tube of heat interchanger 21 and cooling device 22, be all connected with heat eliminating medium, the heat that this heat eliminating medium carries the synthetic gas of flow through heat interchanger 21 and cooling device 22 reclaims.In the present embodiment, coal water mixture, after coal gasifier 11 burnings are processed, generates with CO and H ₂it is main, the temperature synthetic gas 1350 degrees Celsius of left and right, this synthetic gas generates and carries amount of heat, in the time that synthetic gas is flowed through heat interchanger 21 and cooling device 22, between heat eliminating medium and synthetic gas, carry out exchange heat, the entrained energy of synthetic gas is absorbed by the heat eliminating medium in the heat exchanger tube of heat interchanger 21 and cooling device 22, the heat energy of the synthetic gas in coal water slurry gasification process system is reclaimed again.

(3) second tornado dust collector 60

Referring to shown in Fig. 7 to Fig. 9, heat recovery unit 20 also comprises the second tornado dust collector 60, these second tornado dust collector 60 are connected on the pipeline between the gas outlet of heat interchanger 21 and the air intake opening of cooling device 22, remove the lime-ash carrying in synthetic gas, the structure of the second tornado dust collector 60 in the present embodiment and the structure of the first tornado dust collector 222 complete to, different, import and the Way out of synthetic gas in system of the second tornado dust collector 60 is contrary.Now, the entrance of the second tornado dust collector 60 is through hole 2228, manages 2223 upper port centered by outlet, and concrete connected mode is shown in Figure 1.Synthetic gas is connected with first chamber 22271 tangential direction of the second tornado dust collector 60 from through hole 2228, crude synthesis gas containing lime-ash enters rear screw motion from the through hole 2228 in first chamber 22271, the reliable gravity of bulky grain separates in first chamber 22271 with centrifugal force, prevents oarse-grained dust wearing and tearing guide 2225; Synthetic gas enters second chamber 22272 downwards, in gas solid separation, synthetic gas enters pipe core 2223 inside from the diversion trench of guide 2225, guide 2225 with pipe core 2223 for to be tangentially connected, synthetic gas enters pipe core 2223 after guide 2225 is removed a part of solid particle by inertial dust collection, again carry out helical motion, the reliable gravity of grey solid impurity particle and centrifugal force separate pipe core 2223 is interior; Guide 2225 with pipe core 2223 for to be tangentially connected, and the diversion trench gap of multiple guides 2225 of uniform setting can arrange less, the synthetic gas that makes to carry secretly lime-ash is pressed close at the very start inwall and is formed good helical motion, under gravity and centrifugal action, in addition its inertial dust collection effect, has better separating effect with respect to common cyclone separator; Bottom at pipe core 2223 is provided with block piece, i.e. cone 2226 can effectively prevent that the lime-ash falling from being blown afloat at this due to flow perturbation.

Four, washing unit 30, is connected with heat recovery unit 20, the synthetic gas after heat recovery unit 20 is processed is carried out to carrying out washing treatment, for the later use of synthetic gas is carried out place mat.This washing unit 30 comprises the scrubbing tower 31, water gas conveyer 32, water gas filtrator 33 and the water gas separation vessel 34 that connect successively.

(1) scrubbing tower 31

Shown in Figure 10, this scrubbing tower 31 comprises the 3rd housing 310, downtake 320 and spiral stream guidance blade 330, and wherein, the 3rd housing 310 encloses and forms washing cavities 311, in washing cavities 311, cleansing solution is housed; Downtake 320 extends in washing cavities 311 from the outside of the 3rd housing 310, and the outlet side that is positioned at washing cavities 311 of downtake 320 is arranged on below the liquid level of cleansing solution; Spiral stream guidance blade 330 is arranged on around downtake 320 in the cleansing solution of washing cavities 311, and to form spiral stream guidance passage 340, and the port of giving vent to anger of downtake 320 is lower than spiral stream guidance blade 330.While using the scrubbing tower of the present embodiment, synthetic gas enters in washing cavities 311 from downtake 320, and enter in cleansing solution from the port of giving vent to anger being arranged in cleansing solution of downtake 320, now, synthetic gas rises with the form of the bubble direction to the liquid level of cleansing solution in cleansing solution.Due to the guide functions of spiral stream guidance blade 330, the flow-guiding channel that the bubble that synthetic gas forms forms along spiral stream guidance blade 330 moves to the liquid level direction of cleansing solution, increase run duration and the distance of bubble in cleansing solution, now, the dust that cleansing solution can carry bubble carries out the longer time, effectively washing more fully, and then wash out more dust, make the bottom of ash fall at washing cavities 311, meanwhile, due to the guide effect of spiral stream guidance passage 340, bubble can be stretched and be strip, increase the contact area of bubble and cleansing solution, strengthen the clean result of cleansing solution to synthetic gas.In addition, spin in the process of moving at synthetic gas bubble, due to centrifugal action, in bubble, dust gets rid of to the internal face direction of washing cavities 311, it is moistening and wash out that the contact interface that is thrown to bubble and cleansing solution when dust is just washed liquid, thereby effective synthetic gas and dust separation are opened, realized the abundant washing to synthetic gas, and further improve the clean result of cleansing solution to synthetic gas.

Preferably, in the present embodiment, the outward flange away from downtake 320 of spiral stream guidance blade 330 is close to the internal face of washing cavities 311.In the time that synthetic gas enters in cleansing solution from the port of giving vent to anger of downtake 320, prevent that the bubble being formed by synthetic gas from flowing out from the gap between the outward flange of spiral stream guidance blade 330 and the internal face of washing cavities 311, improve the clean result of scrubbing tower to synthetic gas.More preferably, spiral stream guidance blade 330 spirals and is fixed on downtake 320, make all bubbles that formed by synthetic gas all can only from spiral stream guidance passage 340, flow and can rise to the liquid level of cleansing solution, further improve the clean result of scrubbing tower to synthetic gas.

Refer again to shown in Figure 10, washing cavities 311 in the present embodiment is column cavity, downtake 320 comprises the first straight length 321 and the second straight length 322, and wherein the first straight length 321 is perpendicular to the 3rd housing 310 and extend to the inside of washing cavities 311 from the outside of the 3rd housing 310; The second straight length 322 is arranged along the axis of column cavity, and one end that is positioned at washing cavities 311 of the upper end of the second straight length 322 and the first straight length 321 is connected, the lower end of the second straight length 322 extends to the bottom of washing cavities 311, makes the cleansing solution can be to washing fully from downtake 320 synthetic gas out.

Preferably, spiral stream guidance blade 330 spirals and extends to the liquid level of cleansing solution from the lower end of the second straight length 322, can extend as much as possible the run duration of bubble in cleansing solution, and the synthetic gas in bubble can be washed liquid washing more fully.

Preferably, the bottom of column cavity is funnel-shaped structure, after the dust on surface in synthetic gas bubble is washed out, can deposit to the bottom of funnel-shaped structure, and its lowest position of funnel-shaped structure is provided with scum pipe 350, this scum pipe 350 extends to the outside of the 3rd housing 310 from the bottom of funnel-shaped structure, thereby the lime-ash of washing cavities 311 bottoms is discharged to washing cavities 311.

In the present embodiment, the other end place that the first straight length 321 is positioned at the 3rd housing 310 outsides is provided with Venturi scrubber 360, and the position of the close liquid level of scrubbing tower is provided with a leakage fluid dram, and leakage fluid dram place is provided with a Quench water pump.In use procedure; Quench water pump is sent a part of cleansing solution of scrubbing tower into Venturi scrubber 360; when synthetic gas enters into downtake 320 when interior from Venturi scrubber 360; the fresh water (FW) that chilled water pumping comes can make in synthetic gas entrained solid particle fully wetting; when synthetic gas enters washing when strong; solid particle can be deposited in the bottom of washing cavities 311 under the effect of self gravitation; and then excrete out from scum pipe 350; Residue extraction pipeline can be according to actual conditions, select continuously outer row or regular intermittent outer row.

Refer again to shown in Figure 10, the scrubbing tower of the present embodiment also comprises the solid valve formula column plate 370 of polylith, the solid valve formula column plate 370 of polylith is fixedly installed on the inwall of washing cavities 311 and perpendicular to the axis of column cavity, the upper end of the solid valve formula column plate 370 of polylith be provided with condensed fluid entrance, when pass into condensed fluid in condensed fluid entrance time, the synthetic gas rising is upward through the solid valve formula column plate 370 of polylith along the annular space of downtake 320, carry out reverse contact with condensed fluid, the synthetic gas after cleansing solution washing is washed again.

The top of washing cavities 311 is provided with scrubbing tower syngas outlet 380, after the washing of cleansing solution and the washing of solid valve formula column plate 370, flows out from the top of washing cavities 311.

Scrubbing tower also comprises demister 390, this demister 390 is fixedly installed in washing cavities 311, and between the solid valve formula column plate 370 of polylith and scrubbing tower syngas outlet 380, carry out gas-liquid separation, remove the mist being entrained in synthetic gas, avoid from scrubbing tower syngas outlet 380 synthetic gas out from carrying a large amount of cleansing solutions.

In the present embodiment, in the time that scrubbing tower normally moves, spiral stream guidance blade 330 main bodys are all submerged in water, due to the helical structure of spiral stream guidance blade 330 main body uniquenesses, after making synthetic gas export out from downtake 320, upwards do along spiral stream guidance blade 330 after a few helical motion, just pass water layer; Due to the helical structure of spiral stream guidance blade 330 main body uniquenesses, synthetic gas mainly moves in cleansing solution with elongated strip bubble, with respect to the mode that large strand bubble rises in scrubbing tower water-bath of synthetic gas in prior art, the synthetic gas of helical motion will have larger contact area with water, like this, with respect to prior art, in the present invention, the longer contact area of the stroke of synthetic gas in water-bath is longer larger duration of contact, makes in synthetic gas solid particle elute effect better; Most of solid particles sediment of synthetic gas separates with synthetic gas in water-bath.

The air intake opening of the scrubbing tower 31 of the present embodiment is connected by the 7th pipeline 107 with the gas outlet of cooling device 22; synthetic gas after heat recovery is washed; on the 7th pipeline 107, be provided with porcelain filter 70, again the granule dust in separating synthetic gas.

The entrance of water gas conveyer 32 is connected by the 9th pipeline 108 with the outlet of scrubbing tower 31.The entrance of water gas filtrator 33 is connected by the tenth pipeline 109 with the outlet of water gas conveyer 32.The entrance of water gas separation vessel 34 is communicated with by the 11 pipeline 110 with the outlet of water gas filtrator 33.

Synthetic gas after scrubbing tower 31 washings still carries a small amount of solid particle even impurity and the aqueous water that can make transformation catalyst poisoning and deactivation; therefore after water gas conveyer 32, be provided with water gas filtrator 33 and water gas separation vessel 34; further remove solid particle and aqueous water that synthetic gas carries; synthetic gas just enters downstream transforms device after water gas filtrator 33 and water gas separation vessel 34; thereby better protect the transformation catalyst in downstream, ensure the stable operation of downstream unit.

Five, part synthetic gas reflux unit 50, protects the each structure in heat recovery unit 20.

Coal water slurry gasification process system also comprises part synthetic gas reflux unit 50, and part synthetic gas reflux unit 50 comprises the 8th pipeline 51 and compressor 52.Wherein the first end of the 8th pipeline 51 is connected on the duct section between porcelain filter 70 and the scrubbing tower 31 of the 7th pipeline 107, compressor 52 is arranged on the 8th pipeline 51, and the second end of the 8th pipeline 51 is connected with the low temperature synthetic gas entrance 117 of coal gasifier 11; Compressor 52 is arranged on the 8th pipeline 51.Very low through the synthetic gas of cool stream to the seven pipelines 107, about 390 DEG C of left and right, now, the setting of the 8th pipeline 51 can be by the synthetic tedge 116 that is delivered to coal gasifier 11 of low temperature, fully mixing with the synthetic gas just flowing out from firing chamber, can reduce the temperature of synthetic gas flowing out from gas stove, avoid the excess Temperature of synthetic gas and damage the follow up device such as heat interchanger 21, the second tornado dust collector 60, cooling device 22 and scrubbing tower 31 in coal gasifier 11 downstreams.The setting of compressor 52 can be compressed the synthetic gas after cooling, is convenient to the synthetic gas of low temperature to be delivered to coal gasifier 11.

Six, usage on black water unit 40, is connected with washing unit 30, and the Heisui River staying after washing synthetic gas is processed, and avoids contaminated environment.

The Heisui River of coal gasifier 11 and scrubbing tower 31, by level Four flash distillation, parses sour gas, and the Heisui River of slag bath, by two-stage vacuum flash distillation, flashes off toxic and harmful.Flash system is divided into high pressure flash, low pressure flash, the first vacuum flashing and the second vacuum flashing.

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, the flash distillation processing of low pressure flash chamber 44 and vacuum flasher 45, and this processing procedure is consistent with existing Texaco Coal Gasification Process.After flash distillation is processed, Heisui River enters carries out sedimentation in subsider 41.

The usage on black water unit 40 of the present embodiment has the pond 42 of grinding, grinds in pond 42 and is provided with and grinds pond pump 47, grinds between pond pump 47 and subsider 41 and is connected by the 12 pipeline 100, and be provided with operation valve 200 on the 12 pipeline 100.In prior art, the buck that grinds pond 42 returns to subsider 41 and the shared pipeline of slag pool pump outlet, and phase mutual interference, affects pumping, and makes the water quality of gasification ash water be subject to larger impact.Lay separately in the present invention and grind pond pump 47 to the 12 pipeline 100 of subsider 41, like this, the slag bath water that slag pool pump is got and go the grinding water of subsider 41 not interfere with each other, contributes 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, sedimentation is carried out in the Heisui River of flowing out from vacuum flasher 45 subsider 41, the higher mud of subsider 41 bottom solid content, and deliver to vacuum filter from subsider 41 and carry out filter dehydration, form filter cake, and filter cake is sent to battery limit (BL); The cake moisture that vacuum filter filters out is at least more than 50%, and this part lime-ash filter cake after vacuum filter water suction enters cinder exsiccator 46 further to carry out sending processing outside after drying and dehydrating.The primary water overflow on subsider 41 upper stratas is to ash water tank 48, recycling.

In order to accelerate the settling velocity of Heisui River in subsider 41, in subsider 41, add flocculating agent.Thin ash that subsider 41 settles down (Gu the higher mud of amount or claim Heisui River also can) be sent to vacuum band-type filter machine 410 by subsider underflow pump 49.The primary water on subsider 41 tops overflows to ash water tank 48 and recycles.

According to embodiments of the invention, a kind of urgent interlock shutdown method of coal water slurry gasification process system is provided, the coal water slurry gasification process system of the present embodiment is above-mentioned coal water slurry gasification process system.In the present embodiment, the urgent interlock shutdown method of coal water slurry gasification process system comprises: when the absolute value of the rate of temperature change of the absolute value of the rate of temperature change of the absolute value of the rate of temperature change of coal gasifier 11, the oxygen channel that is connected with coal gasifier 11 and the synthetic gas that flows out from scrubbing tower 31 is during all higher than the first preset value, coal water slurry gasification process system is stopped; And/or when the absolute value of the pressure change rate of the absolute value of the pressure change rate of the absolute value of the pressure change rate of coal gasifier 11, oxygen channel and the synthetic gas that flows out from scrubbing tower 31 is during all higher than the second preset value, coal water slurry gasification process system is stopped; And/or in the time that abnormal conditions occur compressor 52, coal water slurry gasification process system is stopped; And/or in the oxygen channel being connected with coal gasifier 11, in the time of oxygen gas flow rate generation abnormal conditions in the oxygen pipeline of center, coal water slurry gasification process system is stopped.It should be noted that, the oxygen channel being connected with coal gasifier 11 is here above-mentioned the first tributary pipeline 301a and the second tributary pipeline 302a, and central oxygen air pipe is the first tributary pipeline 301a.According to the method for the present embodiment, maybe must stop to occur the position of accident in conjunction with the accident that easily occurs in coal water slurry gasification process system, it is coal gasifier 11, oxygen channel, compressor 52 and from scrubbing tower 31, in conjunction with rate of temperature change, pressure change rate and occur that the condition of abnormal conditions realizes the condition of the urgent interlock shutdown of coal water slurry gasification process system, can carry out emergency shut-down control device to coal water slurry gasification process system exactly, ensure the operation stability of coal water slurry gasification process system, avoid the generation of accident, can control accurately whole system, ensure operating personnel's personal safety.When real work, as long as coal water slurry gasification process system meets above-mentioned any one condition, control center's (not shown) of coal water slurry gasification process system is carried out shut-down operation with regard to control system.

In actual production process, with respect to other positions, coal gasifier 11 and the oxygen feeding pipeline being connected with charging aperture 113, that quick-fried frequency occurs to dodge is more for the first tributary pipeline 301a and the second tributary pipeline 302a, and also exist oxygen to press i.e. the first variable valve 36a of fluctuation and coal gasifier 11 burner oxygen pipeline valves, the second variable valve 38a, and first check (non-return) valve 37a and the second check (non-return) valve 39a hidden danger of leaking in damaging, now the interior synthetic gas of coal gasifier 11 will be played a reversed role into oxygen feeding pipeline moment, by near the oxygen pipeline generation detonation first making charging aperture 113, at this moment, high and the low interlock shutdown of pressure height with respect to temperature, rate of temperature change and pressure change rate are by the important parameter that is the accident of reacting sooner, in the time there is detonation, the process that temperature raises and pressure changes, although this time is very short, but temperature and pressure reaches interlocking, value needs the time, and within this of short duration time, detonation is by the more oxygen pipeline that spreads to being exceedingly fast, cause larger security incident, in deflagration, temperature and pressure variation is exceedingly fast greatly, pass through computer system, temperature and pressure rate of change just can draw in the very short time, therefore set temperature rate of change interlock shutdown in the present embodiment, cut off rapidly the each valve of oxygen pipeline and set up elevated pressure nitrogen envelope, can stop effectively faster spreading and the expansion of accident of detonation.Because a kind of in the urgent interlock shutdown method of the present embodiment controls according to rate of temperature change, for the temperature that makes system can not undyingly rise, avoid excess Temperature and cause the blast of system.Therefore, in the present embodiment, when the temperature of coal gasifier 11 higher than the temperature of the 3rd preset value or oxygen channel higher than the temperature of the 4th preset value or the synthetic gas that flows out from scrubbing tower 31 during higher than the 5th preset value, coal water slurry gasification process system is stopped, reduce the too high and potential safety hazard brought of system temperature.The 3rd preset value, the 4th preset value and the 5th preset value in the present embodiment can be determined according to test, meeting is difference with the variation of the each structure in coal water slurry gasification process system, taking the coal gasifier 11 of 5.5MPa as example, in the time that coal gasifier 11 exceedes 1800 DEG C or the temperature of oxygen channel during higher than 260 DEG C or the temperature of the synthetic gas flowing out from scrubbing tower 31 during higher than 280 DEG C, all need to make system to 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 within the scope of 0.4 DEG C/ms to 0.6 DEG C/ms, for example 0.3 DEG C/ms, more preferably, the second preset value is in the scope of 9kpa/ms to 11kpa/ms, and for example 10kpa/ms, avoids intrasystem temperature variation and pressure to change too fast and cause that quick-fried phenomenon appears dodging in system.

Similarly, high and the low interlock shutdown of pressure height with respect to temperature, pressure change rate is by the important parameter that is the accident of reacting sooner, in the time there is detonation, the process that temperature raises and pressure changes, although this time is very short, but temperature and pressure reaches interlocking, value needs the time, and within this of short duration time, detonation is by the more oxygen pipeline that spreads to being exceedingly fast, cause larger security incident, in deflagration, temperature and pressure variation is exceedingly fast greatly, pass through computer system, temperature and pressure rate of change just can draw in the very short time, therefore pressure change rate interlock shutdown is set, cut off rapidly the each valve of oxygen pipeline and set up elevated pressure nitrogen envelope, can stop effectively faster spreading and the expansion of accident of detonation.Because a kind of in the urgent interlock shutdown method of the present embodiment controls according to pressure change rate, the pressure of system can not undyingly rise, and causes system blast for fear of hypertonia.Therefore, in the present embodiment, when the pressure of coal gasifier 11 during higher than the 8th preset value, all needs to make coal water slurry gasification process system to stop higher than the pressure of the 7th preset value or the synthetic gas that flows out from scrubbing tower 31 higher than the pressure of the 6th preset value or oxygen channel.The 6th preset value, the 7th preset value and the 8th preset value in the present embodiment determined according to test, meeting is difference with the variation of the each structure in coal water slurry gasification process system, taking the coal gasifier 11 of 6.5MPa as example, in the time that coal gasifier 11 exceedes 6.75MPa or the temperature of oxygen channel during higher than 6.75MPa or the temperature of the synthetic gas flowing out from scrubbing tower 31 during higher than 6.75MPa, all need to make system to realize urgent interlock shutdown.

Because in technique of the present invention, after cooled synthetic gas (about 390 DEG C of left and right) leaves porcelain filter 70, some turns back to the high-temperature synthesis gas (about 1300 DEG C of left and right) that enters into coal gasifier 11 tedges 116 coal gasifier 11 is generated after by compressor 52 superchargings and carries out Quench, make it high-temperature synthesis gas temperature and be down to 930 DEG C of left and right, the operation if compressor 52 abends, do not have the high-temperature synthesis gas of 1300 DEG C of left and right of Quench directly to enter heat interchanger 21, the second tornado dust collector 60, the follow up device such as cooling device 22 and scrubbing tower 31, thereby will cause on the impact of equipment and normal damaging property of production the generation of security incident, therefore need to arrange compressor 52 exception parking interlockings in the present embodiment.The abnormal conditions of compressor 52 comprise: the top hole pressure of compressor 52 is greater than the 9th preset value; And/or the absolute value of pressure reduction between the outlet of compressor 52 and coal gasifier 11 is higher than the tenth preset value or lower than the 11 preset value; And/or the absolute value of the pressure change rate of compressor 52 is greater than the 12 preset value.The 9th preset value, the tenth preset value, the 11 preset value and the 12 preset value in the present embodiment all determined according to experiment, taking the coal gasifier 11 of 6.5MPa as example, the 9th preset value is that 7.2 ± 0.5MPa, the tenth preset value are that 1.5 ± 0.5MPa, the 11 preset value are that 0.5MPa and the 12 preset value are 2kpa/ms.

Preferably, the 12 preset value in the scope of 1.8kpa/ms to 2.2kpa/ms, for example 2.0kpa/ms.

In the oxygen channel being connected with coal gasifier 11, central oxygen feed channel, i.e. the first direct current pipeline 301a accident of more easily blasting, therefore, also need separately the working condition at oxygen channel place, center to be carried out to independent monitoring, when Ji Dang center oxygen channel generation abnormal conditions, also need to make coal water slurry gasification process system to stop.Specifically, central oxygen feed channel, the oxygen gas flow rate generation abnormal conditions in the first tributary pipeline 301a comprise: oxygen gas flow rate exceedes the 13 preset value, when the 3rd preset value can be set as at full capacity 130% of normal flow, taking 6.5Mpa coal feeding amount as the gasification furnace of 1500 tons is as example, at full capacity time, normal total oxygen gas flow rate is 42400Nm ³about/h, central oxygen flow velocity the oxygen normal flow in the first tributary pipeline 301a at 6600Nm ³/ h left and right, now the oxygen gas flow rate in the first tributary pipeline 301a exceedes 6600Nm ³30% of/h is 8580Nm ³/ h left and right just makes this system shutdown.

In coal gasifier 11 operational processs, the instantaneous pressure of coal gasifier 11, the oxygen channel being connected with coal gasifier 11 and the synthetic gas that flows out from scrubbing tower 31 is that real-time pressure can be recorded by pressure transducer (or claiming tensimeter), real-time pressure signal or pressure data that pressure transducer records are sent to control center, control center's synchronometer calculates the rate of change of pressure, pressure curve over time can be made according to transmitting real-time pressure data by control center, and this slope of a curve is exactly pressure change rate.

In coal gasifier 11 operational processs, the transient temperature of coal gasifier 11, the oxygen channel being connected with coal gasifier 11 and the synthetic gas that flows out from scrubbing tower 31 is that real time temperature can have temperature sensor (or claiming thermometer) to record, real time temperature signal or temperature data that temperature sensor records are sent to control center, control center calculates the rate of change of temperature, temperature curve over time can be made according to transmitting real-time temperature data by control center, and this slope of a curve is exactly rate of temperature change.

Similarly, pressure that compressor 52 exports, temperature variation and and coal gasifier 11 between pressure reduction be delivered to control center after also can detecting by pressure transducer and temperature sensor and process, and then the ruuning situation of the whole coal water slurry gasification process system of Real-Time Monitoring, there is to make when abnormal system shutdown at compressor 52.

The urgent interlock shutdown method of coal water slurry gasification process system of the present invention can effectively be avoided the synthetic gas in coal gasifier to carry pulverized coal particle playing a reversed role and form and dodge quick-fried potential safety hazard into oxygen pipeline, makes its premium properties of maintenance that charging aperture can the longer time.The present invention is in conjunction with the structure that easily occurs accident in coal water slurry gasification process system, be coal gasifier, oxygen channel, compressor and from scrubbing tower, in conjunction with rate of temperature change, pressure change rate and occur that the condition of abnormal conditions realizes the condition of the urgent interlock shutdown of coal water slurry gasification process system, can carry out emergency shut-down control device to coal water slurry gasification process system exactly, ensure the operation stability of coal water slurry gasification process system, avoid the generation of accident, can control accurately whole system, ensure operating personnel's personal safety.When real work, as long as coal water slurry gasification process system meets above-mentioned any one condition, the control center of coal water slurry gasification process system carries out shut-down operation with regard to control system.

The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any amendment of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.

Claims (8)

1. a urgent interlock shutdown method for coal water slurry gasification process system, is characterized in that, comprising:

When the absolute value of the rate of temperature change of the absolute value of the rate of temperature change of the absolute value of the rate of temperature change of coal gasifier (11), the oxygen channel that is connected with described coal gasifier (11) and the synthetic gas that flows out from scrubbing tower (31) is during all higher than the first preset value, coal water slurry gasification process system is stopped; And/or

When the absolute value of the pressure change rate of the absolute value of the pressure change rate of the absolute value of the pressure change rate of coal gasifier (11), described oxygen channel and the synthetic gas that flows out from described scrubbing tower (31) is during all higher than the second preset value, described coal water slurry gasification process system is stopped; And/or

In the time that abnormal conditions occur compressor (52), described coal water slurry gasification process system is stopped; And/or

In described oxygen channel, in the time of oxygen gas flow rate generation abnormal conditions in the oxygen pipeline of center, described coal water slurry gasification process system is stopped.

2. the urgent interlock shutdown method of coal water slurry gasification process system according to claim 1, it is characterized in that, the temperature of the synthetic gas flowing out higher than the 4th preset value or from described scrubbing tower (31) higher than the temperature of the 3rd preset value or described oxygen channel when the temperature of coal gasifier (11) during higher than the 5th preset value, stops coal water slurry gasification process system.

3. the urgent interlock shutdown method of coal water slurry gasification process system according to claim 1, is characterized in that, described the first preset value is within the scope of 0.4 DEG C/ms to 0.6 DEG C/ms.

4. the urgent interlock shutdown method of coal water slurry gasification process system according to claim 1, it is characterized in that, the pressure of the synthetic gas flowing out higher than the 7th preset value and from described scrubbing tower (31) higher than the pressure of the 6th preset value, described oxygen channel when the pressure of coal gasifier (11) during higher than the 8th preset value, stops described coal water slurry gasification process system.

5. according to the urgent interlock shutdown method of the coal water slurry gasification process system described in any one in claim 1 to 4, it is characterized in that, the abnormal conditions of described compressor (52) comprising:

The top hole pressure of described compressor (52) is greater than the 9th preset value; And/or

The absolute value of the pressure reduction between the outlet of described compressor (52) and described coal gasifier (11) is higher than the tenth preset value or lower than the 11 preset value; And/or

The absolute value of the pressure change rate of described compressor (52) is greater than the 12 preset value.

6. the urgent interlock shutdown method of coal water slurry gasification process system according to claim 1, is characterized in that, the oxygen gas flow rate generation abnormal conditions in described central oxygen feed channel comprise: the oxygen gas flow rate in described oxygen channel exceedes the 13 preset value.

7. the urgent interlock shutdown method of coal water slurry gasification process system according to claim 1, is characterized in that, described the second preset value is in the scope of 9kpa/ms to 11kpa/ms.

8. the urgent interlock shutdown method of coal water slurry gasification process system according to claim 5, is characterized in that, described the 12 preset value is in the scope of 1.8kpa/ms to 2.2kpa/ms.