CN110734786B

CN110734786B - Multi-pollution source integrated treatment system for normal and low pressure coal gas

Info

Publication number: CN110734786B
Application number: CN201910898570.XA
Authority: CN
Inventors: 周列
Original assignee: Shanghai Jingye Environmental Protection And Energy Technology Co ltd
Current assignee: Shanghai Jingye Environmental Protection And Energy Technology Co ltd
Priority date: 2018-11-22
Filing date: 2019-09-23
Publication date: 2024-06-04
Anticipated expiration: 2039-09-23
Also published as: CN110734786A; CN110734785B; CN110734785A

Abstract

The invention provides a multi-pollution source integrated treatment system for normal and low pressure coal gas and a multi-pollution source integrated treatment system for coal gas, wherein the reverse pressurizing ash removing area of a self-cleaning filter is used for vibrating dust, glue and salt adsorbed outside the filter bag to shake off by rotating a double-arm reverse pressurizing gas reverse blowing filter bag; the dry dedusting and desalting area is provided with a filter bag and a filter membrane in a circumferential direction to physically filter dust, glue and salt in the gas; the pressure atomization area is used for adjusting the temperature and capturing aerosol through atomized medicament and water, promoting and realizing the growth of aerosol droplets, removing glue and tar through physical filtration, storing ash and discharging ash, and controlling ash, glue and salt. The invention adopts the rotary double-arm reverse pressurizing recoil ash cleaning technology and combines the high-efficiency nozzle, the single-tank treatment air volume can reach 45000 Nm ³/h, the whole structure is more compact, and the transmission component and the instrument configuration are greatly reduced.

Description

Multi-pollution source integrated treatment system for normal and low pressure coal gas

Technical Field

The invention relates to the technical field of industrial coal gas, in particular to a multi-pollution-source integrated treatment system for normal and low-pressure coal gas and a multi-pollution-source integrated treatment system for coal gas, which are suitable for efficiently filtering substances such as dust, glue, salt and the like in the normal and low-pressure coal gas system.

Background

In the coal gas industry of China, the proportion of the normal and low pressure coal gas processes to the whole gas making process is up to more than 60%. The process has the obvious advantages of simple gas making process, low investment and the like, but has the same obvious defects, particularly huge environmental protection pressure, and is mainly characterized by large amount of water slag, waste water which is difficult to treat and has extremely high treatment cost and serious aerosol emission, and the process can cause great harm to the environment and posts, and is surely eliminated without fundamental change.

The normal low pressure gas making process flow (shown in figure 1) commonly adopted at home at present basically comprises the following steps: five technological processes of normal pressure gasification, cyclone separation, waste heat recovery, washing separation and cooling recovery.

Raw gas composition: the carbon in the raw material coal is incompletely combusted under the combined action of oxygen (air, oxygen enrichment, pure oxygen) and water vapor within a certain temperature range to generate raw coke oven gas,

C+O₂→CO

C+H₂O→H₂+CO

The combustion products mainly comprise effective components such as CO, H ₂、CH₄ and the like, substances such as associated phenol, H ₂S、HCN、NH₄ and the like and a large amount of solid particles.

The main treatment process (shown in figure 1) at the present stage: the high-temperature raw gas enters a waste boiler process for heat exchange after large particles are removed through cyclone dust removal, low-pressure steam is produced as a byproduct, the exhaust gas temperature after the waste heat boiler treatment is generally 0-150 ℃, the raw gas enters a washing tower for removing impurities and cooling, and the raw gas enters a back-stage process; the washing liquid is recycled by means of sedimentation, filtration, cooling and the like, and part of incremental wastewater generated due to incomplete conversion of water vapor is discharged after water treatment.

In the normal low pressure gas making process flow as shown in fig. 1, a row-blown filter bag and a blowing pipe are generally used, which are set as shown in fig. 2, and are set as a single tank 12000Nm ³/row of blowing pipes, wherein a pulse valve 3001 for controlling on-off is provided on a blowing pipe line 3002, the blowing pipe line 3002 is connected to the filter bags 3003, a nozzle is provided correspondingly at a position of about 100mm (millimeters) above the mouth of each filter bag 3003, the nozzle is fixedly connected to the blowing pipe, the pulse valve 3001 is intermittently switched, so that the back-blowing gas flow is finally sprayed through the blowing pipe via the nozzle as required, and the generated gas flow pulse by the spraying causes the filter bags 3003 to swell and the ash outside the filter bags to fall. The system shown in fig. 2 has the technical defects of large filtering area, too many pulse valves, nozzles and large occupied area.

In addition, due to the improvement of environmental protection of production enterprises in the current production and society, the existing gas making process has the following defects:

1) The incremental wastewater treatment difficulty is high, and the toxicity is large: the waste water after washing contains a large amount of particles and coal tar and ammonia nitrogen components, so that the waste water is difficult to treat to reach the emission level through an effective economic means;

2) The circulating cooling water quantity is large, the impurity content and the corrosive components are high, the aerosol generated by the high-volatility organic matters is large, the high-volatility organic matters are quite toxic and have great harm to the environment and the occupational health, and meanwhile, the high-volatility organic matters are also the main components forming PM 2.5;

3) Because a large amount of waste water and waste residues exist, environmental protection production in factories is difficult to ensure, and particularly, whenever rainwater exists, harmful substances such as ammonia nitrogen in a sewer and the like are inevitably discharged, so that the quality of water is seriously influenced, and the pollution of underground water and soil is caused;

4) The existing gas making process has low energy conversion rate and large water consumption.

Disclosure of Invention

Based on the problems in the prior art, the invention provides a self-cleaning filter which is suitable for efficiently filtering substances such as dust, glue, salt and the like in a normal-low pressure coal gas system.

According to a first technical scheme of the invention, a self-cleaning filter is provided, which comprises a reverse pressurizing ash removing area, a dry dedusting and desalting area, a pressure atomizing area and an ash storing and discharging area, wherein the reverse pressurizing ash removing area reversely pressurizes air to reversely blow a filter bag through rotating double arms, so that dust, glue and salt adsorbed outside the filter bag shake off through vibration; the dry dedusting and desalting area is used for physically filtering dust, glue and salt in the gas through a filter bag and a filter membrane which are arranged in a circumferential direction; the pressure atomization area regulates the temperature and captures aerosol through atomized medicament and water so as to promote and realize the growth of aerosol droplets, and the aerosol droplets are matched with physical filtration to remove glue and tar; the ash storage and discharge area is used for storing ash, glue and salt and controlling the ash, glue and salt discharge; the pressure atomization zone is preferably a pressure atomization semi-dry tar removal zone.

The ash storage and discharge area is in a cone shape and is connected with the self-cleaning filter cylinder; a nitrogen gun is arranged on the side wall of the cone of the ash storage and discharge area, and a loading level gauge, a storage temperature measuring device and a discharging level gauge are preferably arranged on the side wall of the cone opposite to the nitrogen gun from top to bottom. The feeding level gauge is used for monitoring the upper limit of stored ash, and when the upper limit of stored ash reaching a high material level is detected, the feeding level gauge can send out an ash discharge starting signal to the self-cleaning filter in the form of digital display, vibration signals, sound alarms and the like. When the stored ash layer reaches the feeding level, opening a lower valve to discharge ash; when the stored ash layer reaches the discharging position, the lower valve is closed, and the ash storage is continued. The nitrogen cannon arranged on the side wall of the cone of the ash storage and discharge area shakes off dust accumulated on the side wall of the cone by means of vibration generated by instant release of nitrogen released at high speed by pulses. The dry dedusting area is dedusted by a cloth bag to finish dedusting and desalting. The mouth part of the filter bag is fixedly connected to the round mouth of the flower plate, a plurality of round mouths are formed in the flower plate, and each round mouth is tightly connected with one filter bag. When the high-speed air flow passes through the filter bag, the dust and gum salt are filtered out.

The self-cleaning filter is characterized in that a round self-cleaning filter cylinder body of the self-cleaning filter is used as a central annular distribution filter bag, the filter bag comprises a support frame and a filter bag outer bag, the cross sections of the support frame and the filter bag outer bag are elliptical or other shapes, the support frame is arranged in the filter bag outer bag and used for supporting the filter bag outer bag, and the support frame is matched with the filter bag outer bag in size. The reverse pressurizing ash removing area comprises a reverse dosing ash removing area, and comprises a nozzle, a rotary blowing arm, a rotary blowing pipe, a sealing part, a motor, a gear transmission mechanism, a blowing steam drum and a pulse valve. The nozzles are disposed along the rotary blowing arm. The reverse pressurizing and ash removing area adopts the rotary double-arm reverse pressurizing and ash removing mode and is characterized by being organically combined with the dry dedusting and salt removing area, so that the ash removing effect with the minimum capacity to the maximum is achieved. The pressure atomization area comprises a dosing box, a dosing pump, a temperature control system and an atomization nozzle, and the dosing box is connected with the atomization nozzle sequentially through the dosing pump and the temperature control system. In the pressure atomization zone, the medicament stored in the medicament adding box is subjected to medicament adding and atomization through a medicament adding pump and an atomization spray nozzle, the common atomization pressure is between 3bar and 4bar, and the flow rate of the medicament adding and spraying is controlled through a temperature control system.

Preferably, the pressure atomization zone further comprises a gas distribution plate, and the gas distribution plate is arranged at the lower part of the atomization nozzle; the atomizing nozzle is arranged on the upper part of the gas distribution plate and the lower part of the filter bag.

The reverse pressurizing ash removing area, the dry dedusting and desalting area, the pressure atomizing area and the ash storing and discharging area are integrated in a cone container; the uppermost part is a reverse pressurizing ash removing area, and the next lower part is a dry dedusting and desalting area; the lower part is a pressure atomization area again, and finally an ash storage and discharge area is formed. The reverse pressurizing ash removing area adopts multi-stage motor gear transmission, so that the rotating speed of the rotating double arms or the rotating multiple arms is less than 5 revolutions per minute.

According to the second technical scheme, the invention provides a coal gas multi-pollution-source integrated treatment system, which comprises a normally low pressure gasification device, a primary gas-solid separation device, a heat exchanger, a gas washing tower, a self-cleaning filter and a water heat exchanger, wherein the normally low pressure gasification device, the primary gas-solid separation device, the heat exchanger, the self-cleaning filter, the gas washing tower and the water heat exchanger are sequentially connected, the pressure atomization area of the primary gas-solid separation device is used as a subsequent treatment device of the normally low pressure gasification device, the heat exchanger is used as a subsequent treatment device of the pressure atomization area of the primary gas-solid separation device, the self-cleaning filter is used as a subsequent treatment device of the heat exchanger, the gas washing tower is used as a subsequent treatment device of the self-cleaning filter, and the water heat exchanger is used as a subsequent treatment device of the gas washing tower.

In the coal gas multi-pollution source integrated treatment system, raw gas is discharged from a normal-low pressure gasification device, and enters a heat exchanger for waste heat recovery after large-particle materials are removed in a pressure atomization area of a primary gas-solid separation device; the crude gas after heat exchange enters a self-cleaning filter to become clean gas, and then enters a gas washing tower to further cool the gas and enter a back-stage flow. And the gas enters a gas washing tower to cool the gas, and then the gas becomes clean gas with the temperature lower than 50 ℃. Preferably, the normal-low pressure gasification device is used for gasifying lump coal and pulverized coal to form raw gas, and comprises a storage tank body, a jacket coaxial with the storage tank body is arranged outside the storage tank body, a first inlet is arranged on the side surface of the storage tank body, a second inlet is arranged on the side surface of the storage tank body, and the second inlet is positioned below the first inlet or below the side surface of the storage tank body; the gasifying agent water vapor inlet is also arranged on the side surface of the storage tank body, and penetrates through the jacket to enter the storage tank body; an incremental washing water inlet and a jacket steam outlet are respectively arranged on the outer side of the jacket; the first inlet penetrates through the jacket and enters the storage tank body, and is used for conveying lump coal and pulverized coal into the storage tank body.

In the coal-to-gas multi-pollution-source integrated treatment system, the self-cleaning filter comprises 4 functional areas, namely an ash storage area at the bottom, a dry dedusting and desalting area at the middle upper part, a pressure atomizing area at the middle lower part and a reverse pressurizing and ash removing area at the upper part, wherein the ash storage area is used for storing filtered dust, and the accumulated dust is discharged downwards through a dry slag outlet after reaching a certain material level; an atomizing nozzle is arranged at the top of the pressure atomizing area, a dosing tank, a dosing pump and a temperature control system are arranged outside the pressure atomizing area, the dosing tank is sequentially connected with the dosing pump, the temperature control system and the atomizing nozzle, and the pressure atomizing area is used for removing tar and aerosol.

Preferably, the scrubber is used for scrubbing and cooling the clean gas to below 50 degrees by using scrubbing water; the gas washing tower comprises a clean gas inlet, a clean gas outlet, a washing water inlet, a washing water outlet and a main gas washing tower tank body, wherein the clean gas inlet is arranged at the bottom of the main gas washing tower tank body, the clean gas outlet is arranged at the top of the main gas washing tower tank body, the washing water inlet is arranged on one side surface of the middle upper part of the main gas washing tower tank body, the washing water outlet is arranged at the bottom of the main gas washing tower tank body, and the washing water outlet is positioned on a horizontal plane slightly lower than the clean gas inlet; an atomization device is arranged in the main tank body of the gas washing tower, and is connected with a washing water inlet and used for atomizing the washing water.

In the third technical scheme of the invention, a multi-pollution source integrated treatment system for normal and low pressure coal gas is provided, which comprises four working procedures of normal pressure gasification, cyclone separation, waste heat recovery, washing separation and cooling recovery: a set of washing and separating procedures consisting of self-cleaning filters and ash bins and waste heat boilers are newly arranged after the waste heat recovery procedure.

Preferably, the inlet of the self-cleaning filter is connected with the hot gas outlet of the waste heat boiler to obtain a high-temperature waste heat gas source cooled by the waste heat boiler, the output port at the upper part of the self-cleaning filter is connected with the direct cooling tower in the cooling recovery procedure, the output port at the lower part of the self-cleaning filter is connected with the ash bin through a conveyer to realize the conveying of waste in the self-cleaning process, and the ash bin discharges accumulated ash together with ash generated in the upstream procedure through a conveying pipeline. Further, the self-cleaning filter comprises a shell, a sensing and detecting control unit, a pressure atomizing unit, an inlet cut-off valve assembly, an outlet cut-off valve assembly back-washing backflushing unit and a filtering unit, wherein the filtering unit is arranged at the middle upper part of the self-cleaning filter and plays a role in filtering from bottom to top.

Compared with the prior art, the bag-type dust collector generally adopts inert gas line pulse back blowing, a group of (standard dry) gas volumes of 45000Nm ³/h are usually 4 single tanks or more, the invention adopts a rotary double-arm reverse pressurizing back flushing ash cleaning technology and combines with a high-efficiency nozzle, the single-tank treatment (standard dry) gas volume can reach 45000Nm ³/h, the whole structure is more compact, and the configuration of moving parts and instruments is greatly reduced.

For 45000Nm ³/h of coal gas, the number of pulse valves adopted by the invention is 1-2, and the total number of nozzles is greatly reduced to 20-30; in the existing line blowing, each line is provided with a pulse valve, at least 4 tanks are needed for 45000Nm ³/h of coal gas, the total number of the pulse valves is more than 32, and the number of the nozzles is more than 448. The capability of the single-tank raw gas treatment of the invention reaches 45000Nm ³/h or more (the capability of the single-tank gas bag dust removal treatment is usually less than 15000Nm ³/h).

Drawings

FIG. 1 is a schematic diagram of a conventional normal low pressure gas production process flow;

FIG. 2 is a schematic diagram of a prior art row-blown filter bag and blowing tube arrangement;

FIG. 3 is a schematic view of the self-cleaning filter of the present invention;

FIG. 4 is a schematic view of the ash storage and discharge area of FIG. 3;

FIG. 5 is a schematic view of the nitrogen monitor of FIG. 4;

FIG. 6 is a schematic view of the pressure atomizing area of FIG. 3;

FIG. 7 is a schematic diagram of the pressure atomizing nozzle in FIG. 6;

FIG. 8 is a schematic view of the gas distribution plate of FIG. 6;

FIG. 9 is a schematic diagram of the dry dedusting and desalting zone of FIG. 3;

FIG. 10 is a connection structure of the cloth bag and the flower plate shown in FIG. 9;

FIG. 11 is a schematic view of the arrangement of the cloth bag shown in FIG. 9;

FIG. 12 is a schematic view of the reverse pressurized ash removal zone of FIG. 3;

FIG. 13 is a schematic illustration of the connection of the nozzle of FIG. 12 to a rotary blowing arm;

FIG. 14 is a schematic illustration of the connection of the purge drum and pulse valve of FIG. 12;

FIG. 15 is a schematic diagram of the connection of the motor and gear train of FIG. 12;

FIG. 16 is a step diagram of a self-cleaning filter using the present invention;

FIG. 17 is a flow chart of the efficient filtration of dust, gum, salt materials in a normal low pressure coal-to-gas system using the self-cleaning filter of the present invention;

FIG. 18 is a schematic illustration of the application of the self-cleaning filter of the present invention to a normal low pressure coal-to-gas system;

FIG. 19 is a schematic diagram of a multi-pollution source integrated treatment process for coal gas using the present invention;

FIG. 20 is a schematic view of the low pressure gasification apparatus of FIG. 19;

FIG. 21 is a schematic view of the primary gas-solid separation device of FIG. 19;

FIG. 22 is a schematic view of the first heat exchanger of FIG. 19;

FIG. 23 is a schematic view of the self-cleaning filter of FIG. 19;

FIG. 24 is a schematic view of the scrubber of FIG. 19;

FIG. 25 is a schematic view of the water heat exchanger of FIG. 19;

FIG. 26 is a schematic diagram of a second coal gas multi-pollution source integrated process according to the present invention;

FIG. 27 is a schematic view of a third coal gas multi-pollution source integrated process according to the present invention;

FIG. 28 is a schematic view of a divided wall cooler;

FIG. 29 is a schematic diagram of a multi-pollution source integrated abatement process for coal gas using a two-stage scrubber process.

FIG. 30 is a schematic view of a fourth embodiment of a coal gas multiple pollution source integrated abatement system in accordance with the present invention;

FIG. 31 is a schematic view of a self-cleaning filter employed in the system shown in FIG. 20.

Detailed Description

The invention is further elucidated below in conjunction with the drawings of the description and examples of the invention are given.

The self-cleaning filter can be applied to a normal-low pressure coal gas system, and has the main functions that: the physical filtration is utilized to remove the particles, salt and coal tar in the raw gas, and the solid particles can be removed by a clean filter to be more than or equal to 99.99 percent, and the tar removing rate is more than or equal to 90 percent. The gas is changed into clean gas after passing through a self-cleaning filter. The technical advantages are as follows: the dry dedusting and desalting area 172, the pressure atomizing area 173, the reverse pressurizing and ash removing area 171 and the ash storing and discharging area 174 are organically combined into a whole, so that the solid particulate matter rejection rate is more than or equal to 99.99 percent, and the tar rejection rate is more than or equal to 90 percent; in addition, in the pressure atomization area 173, the pressure atomization semi-dry tar removal technology is utilized to organically combine the dosing box 31, the dosing pump 1732, the temperature control system 1733, the atomization nozzle 1734 and the gas distribution plate, so as to realize automatic control of the temperature of the flue gas, and the aerosol and tar removal rate of micron and submicron in the flue gas is more than 90% by configuring the atomized liquid control.

The self-cleaning filter of the present invention will be described in detail with reference to the accompanying drawings.

The self-cleaning filter shown in fig. 3 comprises a reverse pressurizing and ash removing area 171, a dry dedusting and desalting area 172, a pressure atomizing area 173 and an ash storing and discharging area 174, wherein the reverse pressurizing and ash removing area 171 reversely blows the filter bag by rotating the double-arm reverse pressurizing gas, so that dust and glue adsorbed outside the filter bag is vibrated to shake off; the dry dedusting and desalting area 172 physically filters dust and salt in the gas through a filter bag and a filter membrane which are arranged in a circumferential direction; the pressure atomizing area 173 regulates the temperature and captures aerosol through the atomized medicament to promote and realize the growth of aerosol droplets, and is matched with physical filtration to remove glue and tar. The ash storage and removal area 174 is used to store the ash glue salt and control the removal of the ash glue and salt.

FIG. 4 is a schematic view of the ash storage and discharge area 174 of FIG. 3, the ash storage and discharge area 174 having a conical shape, the conical ash storage and discharge area being connected to a self-cleaning filter cartridge for storing ash (tar, salt) and discharging ash; when the stored ash layer reaches the feeding level, opening a lower valve to discharge ash; when the stored ash layer reaches the discharging position, the lower valve is closed, and the ash storage is continued. The nitrogen cannon 1744 arranged on the side wall of the cone of the ash storage and discharge area shakes off dust accumulated on the side wall of the cone by the vibration generated by the instant release of the nitrogen released by the pulse at high speed. A nitrogen gun 1744 is arranged on one side wall of the cone, and a loading level gauge 1741, a storage temperature measuring device 1742 and a discharging level gauge 1743 are preferably arranged on the side wall of the cone opposite to the nitrogen gun 1744 from top to bottom; in addition, the loading level gauge 1741, the storage temperature measuring device 1742, and the unloading level gauge 1743 may be provided at appropriate positions.

The loading level indicator 1741 is used for monitoring the upper limit of stored ash, and when the upper limit of stored ash reaching a high level is detected, the loading level indicator 1741 can send out an ash discharge starting signal to the self-cleaning filter in the form of digital display, vibration signals, sound alarms and the like. The discharging level gauge 1743 is used for monitoring the lower limit of stored ash, and when the lower limit of the stored ash reaching the low level is detected, the discharging level gauge 1743 can send out an ash discharge end signal to the self-cleaning filter in the form of digital display, vibration signal, sound alarm and the like. The storage temperature measuring device 1742 is used for detecting temperature and/or moisture of the ash storage and discharge area. The nitrogen cannon 1744 is used for pulsing vibration of the ash storing and discharging area to prevent caking.

Fig. 5 is a schematic structural diagram of a nitrogen gun 1744 in fig. 4, where the nitrogen gun 1744 includes a nitrogen gas bag 441, a pulse valve 442 and a pipeline system 443, the nitrogen gas bag 441 is communicated with the pipeline system 443 via the pulse valve 442, and the nitrogen gas bag 441 may be a high-pressure nitrogen gas bag or a gas source connected to a high-pressure gas supply pipeline, and the pulse valve 442 is opened and closed at a pulse timing to enable gas in the nitrogen gas bag 441 to enter the cone-shaped ash storage and discharge area 174 at a high speed through the pipeline system 443, so as to form pulse high-speed gas impact on the bin wall 444, so that the bin wall 444 generates pulse vibration, thereby preventing caking.

Fig. 6 is a schematic diagram of the pressure atomization zone 173 of fig. 3, wherein the pressure atomization zone 173 includes a dosing tank 1731, a dosing pump 1732, a temperature control system 1733, and an atomizer 1734. The dosing tank 1731 is connected to an atomizer 1734 via a dosing pump 1732 and a temperature control system 1733 in turn. In the pressure nebulization area, the medicament stored in the dosing tank 1731 is dosing nebulized by a dosing pump 1732 and a nebulizing nozzle 1734, typically at a pressure of 3bar to 4bar, and the flow rate of the dosing nebulized is controlled by a temperature control system 1733. Aerosol and tar are captured by controlling the temperature of the aerosolized medicament. The pressure atomizing area 173 further includes a gas distribution plate 1735, the gas distribution plate 1735 being provided at a lower portion of the atomizer head for cutting the entire gas flow into small gas flows, preventing turbulence of the gas flow; the atomizing nozzle 1734 is provided at the upper portion of the gas distribution plate, and at the lower portion of the filter bag 21, and has a main function of atomizing the medicine and capturing aerosol and tar. The atomizer 1734 is preferably a pressure atomizer.

Fig. 7 is a schematic view of an arrangement structure of the pressure atomizing nozzle 1734 in fig. 6. In the pressure atomizing area 173 of the self-cleaning filter, the pressure atomizing spray heads are uniformly distributed on the half circumference of a shell at one side of the self-cleaning filter, and are arranged in a cylinder of the self-cleaning filter through a connecting flange pipeline, so that the purpose is mainly to uniformly atomize, and the atomizing radius is large, so that the purpose of fully capturing aerosol and tar is achieved. In the present invention, 7 parallel pressure atomizing nozzles 1734 (pressure atomizing nozzles connected to the H-port) are preferable, and the spraying directions of the parallel pressure atomizing nozzles 1734 are all parallel to the inside of the self-cleaning filter cylinder; two large-caliber spray nozzles (M-port connected pressure atomizer) are preferably arranged on opposite sides of 7 parallel pressure atomizers 1734 along the radial direction of the self-cleaning filter cylinder. The pressure atomizing spray heads are all connected through pressure atomizing spray head connecting pipelines. The setting positions of the two M-port pressure atomizing spray nozzle connecting pipelines are right-angle, and form a triangular symmetrical relation with the H-port pressure atomizing spray nozzle connecting pipeline which is arranged in the middle.

Fig. 8 is a schematic view of the gas distribution plate of fig. 6, in which the circumference is divided into a plurality of areas by a transverse partition plate 201 and a longitudinal partition plate 202, and the gas flow is divided into small gas flow distributions, so that turbulence is prevented and the filtering efficiency can be improved.

Fig. 9 is a schematic structural view of the dry dust and salt removing area in fig. 3, where dust removal and salt removal are completed by bag dust removal. The mouth of the filter bag 21 is fixedly connected to the round mouth of the flower plate 22, a plurality of round mouths are formed in the flower plate 22, and each round mouth is tightly connected with one filter bag 21. When the air flow passes through the filter bag, the dust and gum salt are filtered out.

Fig. 10 is a connection structure of the cloth bag and the pattern plate shown in fig. 9, and fig. 11 is a schematic arrangement diagram of the cloth bag shown in fig. 9, wherein the distribution of the filter bags of the original row blowing (fig. 1) is changed by distributing the filter bags in a circumferential direction, so that the distribution of the filter bags is more compact, more filter bags are arranged in unit area, and the filtering efficiency is higher than 40%. The filter bag comprises a support frame and a filter bag outer bag, the cross sections of the support frame and the filter bag outer bag are oval-like or other shapes, the support frame is arranged in the filter bag outer bag and used for supporting the filter bag outer bag, and the support frame is matched with the filter bag outer bag in size. The ellipse-like shape is an ellipse-like shape and a racetrack-like shape including straight sections. The support frame main body is a rigid cage frame, and comprises a support opening section, a straight-through section and a tail end section which are directly and rigidly connected in sequence; the support mouth section is a hollow concentric elliptical ring structure, the cross section of the support mouth section is in an inverted concave shape, the inner concentric ring layer and the outer concentric ring layer are in closed connection with each other at the respective upper mouth sections through the sealing layers, the inner concentric ring layer (the inner ring of the keel), the outer concentric ring layer (the outer ring of the keel) and the sealing layers form a hollow area, and the hollow area is adapted to the opening end of the outer bag of the filter bag. The straight-through section of the support frame comprises a straight-through radial rigid support keel and a transverse rigid support keel, wherein the transverse rigid support keel is fixed around the outer periphery or the inner periphery of the straight-through radial rigid support keel. The tail end section of the support frame is of an inverted cone structure, and is composed of rigid support keels, and the rigid support keels comprise an upper keel, a bottom keel and a middle straight-through keel, and the upper keel and the bottom keel are fixedly connected together through the middle straight-through keel. The support frame inside the filter bag is used for supporting the filter bag to prevent the filter bag from collapsing, and simultaneously, the filter bag is helpful for cleaning and redistributing dust cakes.

As shown in fig. 10-11, the outer bag of the filter bag is a straight-through filter bag with an opening at the upper end and a closed bottom end, and the straight-through filter bag is preferably a dust removing cloth bag. The upper end opening of the outer bag of the filter bag comprises a concave annular clamping structure, namely a bag ring. During installation, the flower plate is clamped at the concave annular bag ring. The outer bag of the filter bag comprises a lower section of the filter bag. The fabric of the straight-through filter bag is made of high-efficiency filtering, easy dust stripping and durable materials, and the straight-through filter bag is preferably an aramid or terylene dust collection cloth bag. In use, dust adheres to the outer surface of the outer bag of the filter bag. When the dust-containing gas passes through the filter bag, dust is trapped on the outer surface of the filter bag, and clean gas enters the filter bag through the filter material. Because the filter cloth relies on the thickness filtration of whole filter layer, belongs to depth filtration, consequently the whole filter layer depth direction of straight through filter bag forms three-dimensional loose porous structure by the fibre, from inside and outside loose to dense, forms gradient filtration, and it has advantages such as high dirt volume, long filtration life, low pressure differential.

Further, as shown in fig. 10 to 11, the pattern plate is fastened to the groove (fastening structure, i.e., bag ring) of the outer bag of the filter bag, and the pattern plate is fixed under the fastening of the groove, and is used for integrally fixing the filter bag. At this time, the outer layer of the filter bag is contacted with the pattern plate, and the inner layer of the filter bag is contacted with the supporting frame. Application scene: the flower plate divides the dust removing box body into an upper layer and a lower layer, the upper layer of the flower plate is a clean room, the lower layer of the flower plate is a dust removing and recycling room, and the assembled filter bag is positioned in the dust removing and recycling room; the flower plate is provided with an opening, and the filter bag is vertically arranged at the opening.

The filter bag and the flower plate are installed as follows: the outer bag of the filter bag is slightly inserted into the hole of the pattern plate, meanwhile, the mouth of the outer bag of the filter bag is gripped, and the outer bag of the filter bag is slowly fed into the pattern plate until the outer bag body of the filter bag is naturally vertical; the groove-shaped spring ring (groove (clamping structure) of the outer bag of the filter bag is a bag ring) is tightly held by two hands, the buckling spring ring is in a C shape, one hand holds one side of the embedded C-shaped spring ring, and the other hand holds the C-shaped ring of the bulge and fixes the C-shaped ring on the flower plate side; the other side of the spring ring of the outer bag of the filter bag is stretched and opened slowly, and the groove of the spring ring is just embedded into the inner side of the hole of the pattern plate. After the outer bag of the filter bag is installed, the filter bag support frame is slowly placed into the outer bag of the filter bag, the filter bag support frame is prevented from falling down freely, and the flanging of the filter bag support frame is damaged. The inner concentric ring layer and the outer concentric ring layer of the filter bag support frame are sleeved on the mouth of the filter bag outer bag.

Further, the filter bag is fixedly connected with the tower top base through the cleaning chamber, and the pattern plate is arranged on the tower top base. The clean room is usually fixed connection on the fixed beam at urea prilling tower top, and the other end and dust remover box seal welding. The filter bag is fixedly positioned with the dust removing box body through a pattern plate, the pattern plate divides the dust removing box body into an upper layer and a lower layer, the upper layer of the pattern plate is a cleaning chamber, and the lower layer of the pattern plate is a dust recycling chamber; the flower plate is provided with a plurality of openings, a plurality of filter bags are respectively and vertically arranged at the openings, the lower part of the dust removing box body is provided with an opening, and the upper edge of the dust removing box body is arranged on the cleaning room. And an induced draft fan is further arranged on the cleaning chamber and comprises an air inlet and an air outlet, and the air inlet of the induced draft fan is connected with the cleaning chamber through a pipeline. When the dust removing operation is performed, the induced draft fan continuously pumps out the air in the cleaning chamber above the dust removing box body, so that upward flowing air flow is formed in the urea granulating tower, dust particles are mixed with the air flow and are washed to the filter bags, the dust particles are adsorbed by the filter bags, clean air enters the cleaning chamber through the filter bags and from the openings of the flower plates, and is discharged through the exhaust port of the induced draft fan. The sonic ash remover is preferably arranged on the rigid cylinder wall or the cross beam of the urea prilling tower.

Fig. 12 is a schematic view of the reverse pressurized ash removal zone of fig. 3, which includes a nozzle 1711, a rotary blowing arm 1712, a rotary blowing tube 1713, a sealing portion 1714, a motor and gear drive 1715, a blowing drum 1716, a pulse valve 1717, and a rotary blowing arm stiffener 1718. The nozzle 1711 is disposed along the rotary blowing arm 1712, and in order to enhance the rigidity of the blowing pipe, a rotary blowing arm reinforcing rib 1718 is disposed on the rotary blowing arm 1712, and the rotary blowing arm reinforcing rib 1718 is disposed between the rotary blowing pipe 1713 and the rotary blowing arm 1712, and functions of pulling and fixing; and the number of the rotary blowing arms 1712 is 2-3, preferably 2, along the radial direction of the inner diameter of the self-cleaning filter cylinder, and a plurality of nozzles 1711 are arranged at the lower side of the rotary blowing arms 1712, so that the back-blowing inert gas is uniformly blown into the filter bag through the nozzles 1711. A rotary blowing pipe 1713 is arranged on the central axis of the self-cleaning filter cylinder body, the rotary blowing pipe 1713 is connected with a rotary blowing arm 1712, namely the rotary blowing arm 1712 is connected around the rotary blowing pipe 1713 in an axisymmetric way; a sealing portion 1714 is provided at the junction of the self-cleaning filter cylinder and the rotary blowing arm 1712 to promote the tightness of the self-cleaning filter cylinder. The upper end of the rotary blowing pipe 1713 is connected to a blowing drum 1716 via a pulse valve 1717. The motor and gear drive 1715 rotates the rotary blowing tube 1713 and the rotary blowing double arms 1712, and releases the pressurized inert gas in the blowing drum 1716 to be ejected through the nozzle 1711 at high speed by the timing opening of the pulse valve 1717. Because the motor and gear assembly 1715 is rotating, the nozzles spray over all of the filter bags. The reverse pressurized air flow impacts the lower filter bag and is transferred to the bottom of the filter bag, resulting in ash (tar, salt) and the like adsorbed outside the filter bag falling off to the ash storage area. Wherein the sealing of the gas inside the device from the outside is achieved by means of a sealing portion 1714.

Fig. 13 is a schematic view of the connection of the nozzle of fig. 12 to a rotary blowing arm, with the nozzle 1711 disposed below the rotary blowing arm 1712, the nozzle 1711 and the rotary blowing arm 1712 being connected by bolts or rivets.

FIG. 14 is a schematic illustration of the connection of the purge drum and pulse valve of FIG. 12; the blowing steam drum 1716 is used for storing a large amount of recoil inert gas, and is matched with the pulse opening of the pulse valve 1717, and the middle rotary blowing arm 1712 and the rotary blowing pipe 1713 are used for blowing to the upper part of the cloth bag through the nozzle, so that the ash cleaning by the reverse pressurizing pulse is finally realized.

FIG. 15 is a schematic diagram of the connection of the motor and gear train of FIG. 12; the motor 154 drives the bevel gear pair 153, the bevel gear pair 153 engages the pinion gear 152, the pinion gear 152 engages the bull gear 151, and the desired rotational speed of the rotary blowing arm 1712 is achieved, typically less than 5 rpm.

FIG. 16 is a flow chart of a self-cleaning filter using the present invention, comprising the steps of:

firstly, cutting raw gas into small gas flows by a gas distribution plate;

Secondly, aerosol and tar are captured through atomization by a semi-dry method;

thirdly, removing dust and glue by a dry method;

Fourth, reversely pressurizing to remove ash and discharge dust.

FIG. 17 is a flow chart of the efficient filtration of dust, gum, salt materials in a normal low pressure coal-to-gas system using the self-cleaning filter of the present invention; which comprises the following steps:

a first step of; raw gas enters the self-cleaning filter from a raw gas inlet 4001, and the gas flow is cut by a gas distribution plate 4002

Forming small air flow

A second step; the raw gas captures aerosol and tar under the effect of the atomization 4003 of the semi-dry atomized medicament

Thirdly, performing the following steps; the crude gas is filtered by a filter bag 4004 to remove dust and colloid (containing aerosol) in a dry method and finally discharged from a clean gas outlet 4005

Fourth step; ash and salt (containing aerosol and glue oil) accumulated in the filter bag are blown by the reversely pressurized ash cleaning 4006, and the dust glue falls into the ash storage bin and is discharged through the lower port.

FIG. 18 is a schematic illustration of the application of the self-cleaning filter of the present invention to a normal low pressure coal-to-gas system. The self-cleaning filter 17 is arranged behind the waste heat boiler 43 and in front of the direct cooling tower 46, ash, aerosol and tar in the raw gas are filtered out through the self-cleaning filter, wherein the ash removal rate reaches 99.99%, and the aerosol and tar removal rate reaches 90%. The ash, aerosol and glue oil are transported to ash bin. Thereby purifying the raw gas. Specifically, as shown in fig. 18, a branch pipeline 57 directly connected to the normal pressure gasification furnace 41 is provided on a main pipeline of the cooling tower 48 connected to the waste heat boiler 43, and an evaporator 58 is provided in the branch pipeline, and the incremental water containing oxygen, salt and oil gel, which is outputted from the cooling tower 48, is evaporated and then fed into the normal pressure gasification furnace 1. The provided process flow for integrally treating the multiple pollution sources of the normal and low pressure coal gas comprises the following steps:

A. the lump coal entering the normal pressure gasification furnace 41 forms raw coke oven gas with the temperature of about 350 ℃ under the action of oxygen and water vapor, and the formed raw coke oven gas is continuously input into the cyclone separator 42; the mixed gas containing dust with smaller mass under the cyclone separation effect is led into a waste heat boiler 43 through an output pipeline arranged at the upper part of the cyclone separator for cooling treatment, then the cooled raw gas enters the inner cavity of a shell of the self-cleaning filter from bottom to top through a conveying pipeline connected with an inlet cut-off valve group 52 on the self-cleaning filter 17, after the filtering treatment of a filtering unit 55, particles, salt and aerosol mixed in the raw gas are filtered out, the mixed gas is connected to an input interface a of a direct cooling tower 46 through an outlet cut-off valve assembly 53 arranged at the upper part of the self-cleaning filter and a conveying pipeline connected with the outlet cut-off valve assembly 53, and after the water cooling treatment in the direct cooling tower 46, the formed water gas is conveyed to the subsequent working procedure from an output port b at the upper part of the direct cooling tower 46; meanwhile, the direct cooling tower 46 is communicated with an E interface of the cooling tower through a pipeline arranged on an output port d at the bottom, and is communicated with an input interface c of the direct cooling tower 46 through an output interface F of the cooling tower 48 and a control pump 47 arranged on the output pipeline to form a closed cold source loop;

B. While the step A is carried out, the particulate impurities which are discharged by the self-cleaning filter 17 and are deposited in the lower cavity are communicated with the inner cavity of the ash bin 45 through an output pipeline connected with the self-cleaning filter 17 and a conveying device arranged in the pipeline, and are discharged to the waste conveying main pipe 56 through the outer part of the lower output pipeline of the ash bin for outward transportation;

C. At the same time of carrying out the A, B steps, the lower furnace body of the waste heat boiler 43 is provided with two output interfaces H, I and one input interface J, the output interface H is communicated with the inner cavity of the normal pressure gasification furnace 41 through an output pipeline, and the input interface J of the waste heat boiler 43 is connected with the interface G of the cooling tower 48 through a connecting pipeline;

D. At the same time as the A, B, C step, the normal pressure gasifier 41, cyclone 42, waste heat boiler 43 and ash bin 45 respectively transport the slag and ash with heat value generated during their operation to the waste collection point through the waste transport header 56 via their respective waste discharge pipelines.

The main pipeline of the treatment process, which is communicated with the waste heat boiler 43 through the cooling tower 48, is provided with a branch pipeline 57 which is directly connected with the normal pressure gasifier 41, and an evaporator 58 is additionally arranged in the branch pipeline, and the incremental water which is output by the cooling tower 48 and contains oxygen, salt and oil glue is sent into the normal pressure gasifier 41 after evaporation treatment; in this way, the problem is solved that in the state that the cooling water accumulated in the cooling tower 48 is excessive, the excessive waste water is converted into steam by the evaporator 58 and then sent into the normal pressure gasification furnace 41 to participate in gasification of lump coal.

In addition, according to another technical scheme provided by the invention, the invention provides a coal gas multi-pollution source integrated treatment system and a method, as shown in fig. 19, wherein the coal gas multi-pollution source integrated treatment system comprises a normal low pressure gasification device 11, a primary gas-solid separation device 12, a heat exchanger 13, a gas washing tower 14, a self-cleaning filter 17 and a water heat exchanger 18. The crude gas is discharged from the normal-low pressure gasification device 11, the large-particle materials are removed by the primary gas-solid separation device 12 and then enter the heat exchanger 13 for waste heat recovery, the crude gas after heat exchange enters the self-cleaning filter 17 to become clean gas, and then enters the gas washing tower 14 to further cool the gas and then become clean gas with the temperature lower than 50 ℃ and enter the back-stage flow; the washing water is cooled by the water heat exchanger 18 and then returns to the scrubber tower 14 for recycling. A part of the incremental washing water is recycled to the jacket of the normal-low pressure gasification device 11 and is changed into steam to be recycled to the normal-low pressure gasification device 11, and the other part of the incremental washing water is changed into water steam to be recycled to the normal-low pressure gasification device 11 through the heat exchanger 13; dry ash discharged by the normal low pressure gasification device 11, the primary gas-solid separation device 12, the heat exchanger 13 and the self-cleaning filter 17 is transported to the boiler for secondary blending combustion.

In the system, lump coal, molded coal, pulverized coal and the like form high-temperature raw gas in a normal-low-pressure gasification device 11 under the action of pure oxygen (preferably with purity of more than 99 percent), oxygen-enriched oxygen (preferably with purity of between 50 and 70 percent) air and gasifying agent steam, and the raw gas passes through a primary gas-solid separation device 12 to remove large particles in the raw gas. Then the waste heat enters the heat exchanger 13 to recycle the high temperature waste heat in the crude gas, and the temperature is usually 140-220 ℃. The crude gas after waste heat recovery enters a self-cleaning filter 17 for self-cleaning filtration. During the process, solid particles with the removal rate of more than or equal to 99.99 percent and aerosol and tar substances with the removal rate of more than or equal to 90 percent can be removed. After self-cleaning filtration is changed into clean gas, the clean gas enters the gas washing tower 14 and is cooled to below 50 ℃. And then entering the subsequent process. The gas washing water in the gas washing tower is recycled after being subjected to airtight cooling through a water heat exchanger 18. The increment washing water is recycled to the jacket of the normal low pressure gasification device 11 after being softened and is changed into steam to be recycled to the normal low pressure gasification device 11; dry ash discharged by the normal low pressure gasification device 11, the primary gas-solid separation device 12, the heat exchanger 13 and the self-cleaning filter 17 is transported to the boiler for secondary blending combustion.

As shown in fig. 20, the above-mentioned normal-low pressure gasification device 11 is for gasifying lump coal, pulverized coal, etc. to form a raw gas, and comprises a tank body, a jacket coaxial with the tank body is provided outside the tank body, a first inlet 113 is provided on a side surface (preferably, in the middle and upper direction) of the tank body, a second inlet 114 is provided on a side surface (preferably, in the middle and lower direction) of the tank body, and the second inlet 114 is located below or laterally below the first inlet 113; the gasifying agent water vapor inlet 112 is also provided on the side of the tank body (preferably in the middle lower part) which penetrates the jacket into the tank body; an incremental wash water inlet 117 and a jacket steam outlet 115 are provided outside the jacket, respectively. The first inlet 113 penetrates through the jacket and enters the storage tank body for feeding lump coal/pulverized coal and other materials into the storage tank body.

In the normal-low pressure gasification device 11, lump coal and pulverized coal enter the normal-low pressure gasification device through a first inlet 113, air, oxygen-enriched air or pure oxygen enter through an inlet second inlet 114, gasifying agent water vapor enters through a gasifying agent water vapor inlet 112, raw gas is formed by gasification under the action of gasifying agent and is discharged from a top raw gas outlet 111, and slag is discharged from a bottom first slag discharge port 116. Part of the incremental water from the scrubber outlet enters the incremental water jacket from inlet 117 and becomes steam which is discharged for reuse from outlet 115.

As shown in fig. 21, the primary gas-solid separator 12 is used for separating large particle dust from the raw gas. The raw gas tangentially enters the primary gas-solid separation device from the raw gas inlet 122, large particles contained in the raw gas are settled in the gas-solid separation device under the dual actions of centrifugal force and gravity and are discharged from the slag outlet 123 of the primary gas-solid separation device, and the raw gas from which large particle dust is removed is discharged from the raw gas outlet 121.

As shown in fig. 22, the heat exchanger 13 functions to cool the raw gas to a temperature between 140 and 240 degrees. The incremental washing water is changed into water vapor through heat exchange, and then is returned to the normal-low pressure gasification device 11 to be used as gasifying agent through an inlet 112. The high-temperature raw gas enters the heat exchanger from the raw gas inlet 131, and is discharged from the raw gas outlet 134 after fully exchanging heat with water in the heat exchanger, the temperature is reduced to 140-220 ℃, the increment washing water enters from the inlet 133 and is changed into steam after exchanging heat with the raw gas, and the steam is discharged from the steam outlet 132, and is recycled to the normal-low pressure gasification device 11 to be used as a gasifying agent.

The self-cleaning filter as shown in fig. 23 comprises 4 functional areas, namely an ash storage area 174 at the bottom, a dry dedusting and desalting area 172 at the middle upper part, a pressure atomization area (preferably a pressure atomization semi-dry tar removal area) 173 at the middle lower part and a reverse pressurizing ash removal area 171 at the upper part, wherein the ash storage area 174 is used for storing filtered dust, and the accumulated dust is discharged downwards through a dry slag outlet 17c after reaching a certain material level; an atomizing nozzle 1734 is arranged at the top of the pressure atomizing area 173, a dosing tank 1731, a dosing pump 1732 and a temperature control system 1733 are arranged outside the pressure atomizing area 173, the dosing tank 1731 is sequentially connected with the dosing pump 1732, the temperature control system 1733 and the atomizing nozzle 1734, the pressure atomizing area 173 is used for removing tar and aerosol, the temperature of the flue gas is locally controlled in a certain temperature range suitable for capturing the aerosol according to proportion, and meanwhile, a sufficient amount of fine suspension liquid drops are generated to capture gas glue, tar and the like.

The dry dedusting and desalting zone 172 is used for removing dust and salt, and captures particles (dust) by adopting a physical filtering principle, forms a dust layer with a certain thickness on the surface layer, and captures aerosol and fine liquid drops by utilizing the adsorption effect of porous dust. The reverse pressurized ash removal zone 171 removes ash by pressurization, which uses reverse pressure to shake porous dust down.

Further, the temperature of the raw gas passing through the heat exchanger is 140-240 ℃, the raw gas enters from a raw gas inlet 17A at the side part (near the bottom part of the pressure atomization zone) of the pressure atomization zone of the self-cleaning filter, passes through the pressure atomization zone, the dry dedusting and desalting zone and the reverse pressurizing and ash removing zone 171, and is discharged from a clean gas outlet 17B near the top side surface of the reverse pressurizing and ash removing zone 171 to become clean gas. 99.9% of dust, more than 90% of aerosol and tar contained in the raw gas become porous particles, fall into the ash storage area 174 under reverse pressurization, and are discharged from the dry slag outlet 17C.

The self-cleaning filter has the main functions that: the physical filtration is utilized to remove the particles, salt and coal tar in the raw gas, and the solid particles can be removed by a clean filter to be more than or equal to 99.99 percent, and the tar removing rate is more than or equal to 90 percent. The gas is changed into clean gas after passing through a self-cleaning filter. The technical advantages are as follows: the dry dedusting and desalting area 172, the pressure atomizing area 173, the reverse pressurizing ash removing area 171 and the ash storing area 174 are organically combined into a whole, so that the solid particulate matters can be removed by more than or equal to 99.99 percent, and the tar removing rate is more than or equal to 90 percent; in addition, the pressure atomization area 173 utilizes the pressure atomization semi-dry tar removal technology to organically combine the dosing box 1731, the dosing pump 1732, the temperature control system 1733 and the atomization nozzle 1734 to realize automatic control of the temperature of the flue gas, and the atomization liquid is configured to control, so that the removal rate of aerosol and tar in the micron and submicron level in the flue gas is more than 90 percent.

Compared with the conventional bag-type dust collector generally adopting inert gas line pulse back blowing, the bag-type dust collector for selecting coal gas with a group (standard dry) gas quantity of 45000Nm ³/h is generally 4 single tanks or more, the invention can further adopt a rotary double-arm reverse pressurizing back flushing ash cleaning technology and combine with a high-efficiency nozzle, the single-tank treatment (standard dry) gas quantity can reach 45000Nm ³/h, the whole structure of the invention is more compact, the configuration of moving parts and instruments is greatly reduced, and the device is more stable and safer. The capability of the single-tank raw gas treatment of the invention reaches 40000Nm ³/h or more (the capability of the single-tank gas bag dust removal treatment is usually less than 15000Nm ³/h).

The scrubber tower 14 is used for scrubbing and cooling the clean gas to below 50 ℃ by using the scrubbing water, and meets the requirement of the next process, as shown in fig. 24. The scrubber 14 comprises a clean gas inlet 141, a clean gas outlet 142, a washing water inlet 143, a washing water outlet 144 and a main scrubber tank body, the clean gas inlet 141 is arranged at the bottom of the main scrubber tank body, the clean gas outlet 142 is arranged at the top of the main scrubber tank body, the washing water inlet 143 is arranged at one side surface of the middle upper part of the main scrubber tank body, the washing water outlet 144 is arranged at the bottom of the main scrubber tank body, and the washing water outlet 144 is positioned on a level slightly lower than the clean gas inlet 141; an atomizing device is arranged in the main tank body of the gas washing tower, and is connected with the washing water inlet 143 for atomizing the washing water. The atomizing means is preferably a pressure atomizer.

Preferably, clean gas passing through the self-cleaning filter 17 enters from the bottom clean gas inlet 141, and is discharged from the clean gas outlet 142 after reverse heat exchange of atomized washing water; the washing water enters from the washing water inlet 143 through the pressure atomization nozzle, and the atomized washing water and the high-temperature clean gas exchange heat/wash/cool are changed into high-temperature washing water after being cooled, and then the high-temperature washing water is discharged from the outlet 144.

A water heat exchanger as shown in fig. 25 is connected to the high temperature washing water of the scrubber from the outlet 144, and the water heat exchanger functions to cool and recycle the high temperature washing water in a closed cycle. Preferably, the high-temperature washing water from the washing water outlet 144 of the gas washing tower enters the heat exchanger from the washing water bottom inlet 181, is cooled by the water heat exchanger, is discharged from the washing water upper outlet 182, and is recycled for spraying; the cooling water enters from the cooling water bottom inlet 184 and exits from the cooling water upper port 183.

Further, as shown in fig. 26, a steam storage tank is additionally arranged on the basis of the integrated treatment system for multiple pollution sources of the coal gas. In the coal-to-gas multi-pollution-source integrated treatment system, lump coal and pulverized coal are fed into a normal-low pressure gasification device 11 through an inlet 113 by a coal feeding device; air, oxygen-enriched or pure oxygen enters from the bottom 114 through the air blower by the interface, gasifying agent steam enters from the inlet 112, raw gas formed by gasification under the action of the gasifying agent is discharged from the top 111, and slag is discharged from the bottom 116.

After the partial increment water from the outlet of the gas washing tower enters the increment water jacket from 117 to absorb heat, the partial increment water is changed into water vapor which is discharged from 115 to a storage tank, and then is recycled to the normal-low pressure gasification device 11 to be used as a gasifying agent from 112. The crude gas from the normal-low pressure gasification device 111 enters the primary gas-solid separation device through an inlet tangential line 122, large particles contained in the crude gas are settled in the gas-solid separation device under the dual actions of centrifugal force and gravity and discharged from a slag outlet 123 of the primary gas-solid separation device, the crude gas from which large particle dust is removed is discharged from a crude gas outlet 121, then enters a heat exchanger from a crude gas inlet 131, and is discharged from a crude gas outlet 134 after fully exchanging heat with water in the heat exchanger, the temperature is reduced to 140-220 ℃, part of incremental washing water enters from an inlet 133 and is changed into steam after exchanging heat with the crude gas to be discharged from a steam outlet 132, and then is recycled to the normal-low pressure gasification device 11 to be used as a gasifying agent. The temperature of the raw gas after passing through the heat exchanger is 140-240 ℃ and enters from the inlet 17A at the bottom of the pressure atomization area of the self-cleaning filter, and the raw gas passes through the pressure atomization area and the dry dedusting and desalting area and is changed into clean gas from the outlet 17B near the top. The raw gas contains 99.9% dust, more than 90% aerosol and tar become porous particles, and the porous particles fall into the ash storage area 174 under reverse pressurization and are discharged from the discharge outlet 17C.

Clean gas passing through the self-cleaning filter 17 enters from the bottom clean gas inlet 141, and is discharged from the clean gas outlet 142 after reverse heat exchange of atomized washing water; the washing water enters from the washing water inlet 143 through the pressure atomizer, and becomes high-temperature washing water to be discharged from the outlet 144 after the heat exchange/washing/cooling of the high-temperature clean gas is completed.

The high-temperature washing water from the washing water outlet 144 of the gas washing tower enters the water heat exchanger from the washing water bottom inlet 181, is cooled by the water heat exchanger, is discharged from the washing water upper outlet 182, and is recycled for spraying. The cooling water enters from the cooling water bottom inlet 184 and exits from the cooling water upper port 183.

Compared with the existing separation modes, such as cyclone separation, the primary gas-solid separation device greatly improves the separation efficiency and reduces the service life of equipment; compared with the combined use of the gas washing tower, the sedimentation tank and the cooling tower, the self-cleaning filter and the gas washing tower are used in combination, so that the pollution to the environment is reduced, the occupied area is reduced, the equipment expenditure is saved, and the quality and the efficiency are greatly improved.

In yet another aspect of the invention, an alternative process is provided that uses a divided wall cooler 24A in place of the scrubber 14 and water heat exchanger 18 in the embodiment shown in fig. 26. As shown in fig. 27, the crude gas is discharged from the normal-low pressure gasification device 11, large particles are removed by the primary gas-solid separation device 12, then the crude gas enters the heat exchanger 13 for waste heat recovery, the crude gas after heat exchange enters the self-cleaning filter 17 to become clean gas, and then enters the further dividing wall type cooler 24A to cool the gas and then become clean gas with the temperature lower than 50 ℃ to enter the back-stage flow; part of the condensed water is recycled to the jacket of the normal low pressure gasification device 11 and is changed into steam to the normal low pressure gasification device 11, and the other part of the condensed water is recycled to the normal low pressure gasification device 11 after being changed into water steam in the condensed water heat exchanger 13; the impurities such as dry ash and slag discharged by the normal low pressure gasification device 11, the primary gas-solid separation device 12, the heat exchanger 13 and the self-cleaning filter are transported to the boiler for secondary blending combustion.

As shown in the partition wall type cooler 24A of FIG. 28, the partition wall type cooler 24A cools the clean gas to below 50 ℃ through a partition wall cooling mode (a tube type heat exchanger, a plate type heat exchanger and the like) so as to meet the next process requirement. The clean gas passing through the self-cleaning filter 17 enters from a clean gas inlet 24A3 of the dividing wall type cooler 24A, is cooled by the dividing wall type cooler 24A and is discharged from a clean gas outlet 24A 4; cooling water enters from the washing water inlet 24A1, cooling water is discharged from the cooling water outlet 24A2, and condensed water in the clean gas is discharged from the washing water outlet 24 A5.

The partition wall cooling process has the technical advantages that condensed water in the clean gas is condensed by the partition wall cooler and then recycled, so that the condensate water is prevented from being mixed with other water and is completely isolated from the atmosphere; after the self-cleaning filter is additionally arranged, condensed water in the dividing wall type condenser only contains trace particulate matters, organic matters and water-soluble gases, almost no salt is contained, the quality of washing water is close to the soft water level, the washing water can return to a jacket of the normal-low pressure gasification device, and the washing water can be reused as a gasifying agent to the normal-low pressure gasification device after being changed into water vapor, so that the times and the efficiency of recycling materials are improved.

Further, a two-stage scrubber process (as shown in fig. 29) is adopted in the system and method for integrated treatment of multiple pollution sources of coal gas. The crude gas is discharged from the normal-low pressure gasification device 11, large particles are removed by the primary gas-solid separation device 12 and then enter the heat exchanger 13 for waste heat recovery, the crude gas subjected to heat exchange enters the self-cleaning filter 17 to become clean gas, then enters the first-stage gas washing tower 34B to cool the clean gas to within 5 ℃ above the dew point temperature of the clean gas and then enters the second-stage gas washing tower 34C, part of high-temperature washing water generated during the process enters the jacket of the normal-low pressure gasification device 11 to be changed into steam to be recycled to the normal-low pressure gasification device 11, and the other part of high-temperature washing water enters the heat exchanger 13 to be changed into water steam and then is recycled to the normal-low pressure gasification device; the clean gas cooled by the first stage scrubber 34B is cooled to the desired temperature, typically below 50 degrees celsius, by the second stage scrubber 34C and then enters the subsequent process. The dry ash discharged by the normal low pressure gasification device 11, the primary gas-solid separation device 12, the heat exchanger 13 and the self-cleaning filter 17 is transported to the boiler for secondary blending combustion.

The two-stage gas washing tower can quantitatively control the water inflow of the first-stage gas washing tower, and the water outlet temperature at the lower part of the gas washing tower is highest after the clean gas is cooled to be within 5 ℃ above the dew point temperature of the clean gas. And ensuring the balance between the water yield at the lower part of the gas washing tower and the water yield in the jacket and the heat exchanger of the normal-low pressure gasification device; further, the highest temperature of the washing water entering the jacket and the heat exchanger of the normal-low pressure gasification device is ensured, and the energy is saved.

Further embodiments of the present invention will now be described in detail with reference to the embodiments shown in FIGS. 30-31, wherein FIG. 30 is a schematic illustration of a fourth embodiment of a coal-to-gas multiple pollution source integrated abatement system in accordance with the present invention; FIG. 31 is a schematic view of a self-cleaning filter employed in the system shown in FIG. 30.

According to the fig. 30 and 31, the multi-pollution source integrated treatment system for the normal and low pressure coal gas comprises four processes of normal pressure gasification, cyclone separation, waste heat recovery, washing separation and cooling recovery: a set of washing and separating process consisting of a self-cleaning filter 17 and an ash bin 45 and a cooling and recovering process consisting of a direct cooling tower 46 and a cooling tower 48 which are respectively communicated with the waste heat boiler 43 and the self-cleaning filter 17 are newly arranged after the waste heat recovering process; thus, the pollution-free and leakage-free integrated treatment system for multiple pollution sources of the normal and low-pressure coal gas is formed.

The inlet of the self-cleaning filter 17 is connected with the hot gas outlet of the waste heat boiler 43 to obtain a high-temperature waste heat gas source cooled by the waste heat boiler, the upper outlet of the self-cleaning filter 17 is connected with the direct cooling tower 46 in the cooling recovery procedure, the lower outlet of the self-cleaning filter 17 is connected with the ash bin 45 through a conveyer 49 to realize the conveying of waste in the self-cleaning process, and the ash bin 45 discharges accumulated ash together with ash generated in the upstream procedure through a conveying pipeline.

The direct cooling tower 46 is provided with four external interfaces, wherein an input interface a arranged at the bottom of the lower part of the tower body is connected with an upper output port of the self-cleaning filter, an output interface b at the upper part of the direct cooling tower 46 is a gas output port which is directly communicated with a next procedure, the cooling tower 48 is provided with three interfaces, and an output interface F is connected with an input interface c on the direct cooling tower 46 through a control pump 47; the interface E of the cooling tower 48 is connected with the output interface d at the lower part of the direct cooling tower 46, thereby forming a closed cooling loop between the direct cooling tower 46 and the cooling tower 48; meanwhile, the other port G of the cooling tower 48 is communicated with the waste heat boiler 43.

The self-cleaning filter 17 comprises a shell 59, a sensing and detecting control unit 50, a pressure atomizing unit 51, an inlet cut-off valve assembly 52, an outlet cut-off valve assembly 53, a backwashing backflushing unit 54 and an overflow unit 55, wherein the overflow unit 55 is arranged at the middle upper part of the self-cleaning filter and plays a role in bottom-up filtration.

The practical use shows that: according to the technical scheme, the integrated treatment system for the multiple pollution sources of the normal and low pressure coal gas is provided, and because a plurality of independent devices of the whole set of equipment for manufacturing the water gas form a nearly totally-closed process flow, sewage, ash, waste gas and the like possibly occurring in each process flow can be totally formed into a closed process loop; completely and effectively solves the leakage of various pollutants such as water, gas, ash and the like existing in the operation of the traditional normal and low pressure coal gas production equipment. Has great positive significance for protecting production environment and even urban environment.

In summary, the system and process of the present invention have the fundamental change in the composition of the clean gas after treatment with the self-cleaning filter, which mainly comprises CO, CO ₂、H₂、CH₄, and particles with a content of less than 5mg/Nm ³, and trace amounts of tar and H ₂S、NH₃, and unconverted water vapor. The synthetic gas is changed into semi-water gas needed by the process after water washing.

4) After the self-cleaning filter 17 is additionally arranged, the washing circulating water only contains trace particulate matters, organic matters and water-soluble gases, almost no salt is contained, the quality of the washing water is close to the soft water level, the washing water is introduced into the jacket of the normal low pressure gasification device 11, and the heat exchanger 13 is changed into water vapor to be used as a gasifying agent to be recycled into the normal low pressure gasification device 11.

5) The closed circulation does not discharge to the atmosphere (zero waste gas), the washing water in the prior art contains dust, aerosol, tar and the like, and a large amount of volatile aerosol and organic matters are volatilized to the atmosphere in a ditch, a sedimentation tank and an open cooling tower, so that serious atmospheric pollution is caused.

The water heat exchanger 18 is used for cooling the washing water in the new process, the circulation process is completely closed, any volatile gas and aerosol can not be discharged to the atmosphere, and meanwhile, the pipeline blockage and the heat exchanger blockage can not be caused due to the low content of dust, oil glue and the like in the washing water.

6) The water slag and dry slag are recycled, ash slag generated by an 11-normal low pressure gasification device, a 12-primary gas-solid separation device and a 13-heat exchanger and 17-self-cleaning type filtered and trapped dry ash (carbon-containing ash slag, aerosol, jiao Youlei, salt and the like) are discharged to a designated area through conveying equipment, because the discharged ash slag generally contains fixed carbon and tar components (the calorific value is 3000 kilocalories/kg), the discharged ash slag can be usually returned to a boiler section to be mixed with burning steam, and the fly ash is converted into boiler fly ash for comprehensive utilization through burning; thereby avoiding a great amount of water slag in the waste water washed by the original water washing tower and the water washing tower.

The above is merely a basic implementation method according to the technical solution provided by the inventor, and does not represent the whole of the present application; any such technology that is not substantially modified by those skilled in the art in light of this disclosure should be considered as falling within the scope of the present application.

Claims

1. The integrated treatment system for the multiple pollution sources of the coal gas comprises a normal low-pressure gasification device (11), a primary gas-solid separation device (12), a heat exchanger (13), a gas washing tower (14), a self-cleaning filter (17) and a water heat exchanger (18), and is characterized in that the normal low-pressure gasification device (11), the primary gas-solid separation device (12), the heat exchanger (13), the self-cleaning filter (17), the gas washing tower (14) and the water heat exchanger (18) are sequentially connected, the primary gas-solid separation device (12) is used as a subsequent treatment device of the normal low-pressure gasification device (11), the heat exchanger (13) is used as a subsequent treatment device of the primary gas-solid separation device (12), the self-cleaning filter (17) is used as a subsequent treatment device of the heat exchanger (13), the gas washing tower (14) is used as a subsequent treatment device of the self-cleaning filter (17), and the water heat exchanger (18) is used as a subsequent treatment device of the gas washing tower (14);

The self-cleaning filter comprises a reverse pressurizing ash removing area (171), a dry dedusting and desalting area (172), a pressure atomizing area (173) and an ash storing and discharging area (174), wherein the reverse pressurizing ash removing area (171) reversely pressurizes air to reversely blow the filter bag through rotating the double arms, so that dust, glue and salt adsorbed outside the filter bag are vibrated to shake off; the dry dedusting and desalting area (172) physically filters dust, glue and salt in the gas through a filter bag and a filter membrane which are arranged in a circumferential way; the pressure atomization area (173) regulates the temperature and captures aerosol through atomized medicament and water so as to promote and realize the growth of aerosol droplets, and is matched with physical filtration to remove glue and tar; the ash storage and discharge area (174) is used for storing ash, glue and salt and controlling the ash, glue and salt discharge; the pressure atomization area is a pressure atomization semi-dry tar removal area; the gas washing water in the gas washing tower is circularly used after being subjected to airtight cooling through a water heat exchanger; the increment washing water is recycled to the jacket and the heat exchanger of the normal low pressure gasification device after being softened and changed into steam to be recycled to the normal low pressure gasification device;

the ash storage and discharge area (174) is in a cone shape, and the ash storage and discharge area (174) is connected with the self-cleaning filter cylinder; a nitrogen gun (1744) is arranged on the side wall of the cone of the ash storage and discharge area (174), and a loading level gauge (1741), a storage temperature measuring device (1742) and a discharging level gauge (1743) are arranged on the side wall of the cone opposite to the nitrogen gun (1744) from top to bottom; when the stored ash layer reaches the feeding level, opening a lower valve to discharge ash; when the stored ash layer reaches the discharging position, closing the lower valve to continue storing ash; the nitrogen cannon (1744) arranged on the side wall of the cone shakes off dust accumulated on the side wall of the cone by means of the instant release of pulse nitrogen released at high speed;

The feeding level gauge (1741) is used for monitoring the upper limit of stored ash, and when the upper limit of stored ash reaching a high level is detected, the feeding level gauge (1741) can send out an ash discharge starting signal to the self-cleaning filter in a digital display or vibration signal or sound alarm mode; the discharging level gauge (1743) is used for monitoring the lower limit of stored ash, and when the lower limit of the stored ash reaching the low level is detected, the discharging level gauge (1743) can send out an ash discharge end signal to the self-cleaning filter in the form of digital display or vibration signals or sound alarms;

The rotary blowing arm (1712) is provided with a rotary blowing arm reinforcing rib (1718), and the rotary blowing arm reinforcing rib (1718) is arranged between the rotary blowing pipe (1713) and the rotary blowing arm (1712); the number of the rotary blowing arms (1712) is 2-3 along the radial direction of the inner diameter of the self-cleaning filter cylinder; a plurality of nozzles (1711) are arranged at the lower side of the rotary blowing arm (1712), and the back blowing inert gas is uniformly blown into the filter bag through the nozzles (1711);

In the pressure atomization area of the self-cleaning filter, pressure atomization spray heads are uniformly distributed on the half circumference of a shell at one side of the self-cleaning filter, and the pressure atomization spray heads are arranged in a cylinder of the self-cleaning filter through a connecting flange pipeline; the spraying directions of the pressure atomizing spray heads which are arranged in parallel are all parallel to the inside of the self-cleaning filter cylinder, and the pressure atomizing spray heads are all connected through the pressure atomizing spray head connecting pipeline.

2. The integrated treatment system for multiple pollution sources of coal gas according to claim 1, wherein the dry dedusting area is dedusted by a cloth bag to complete dedusting and desalting; the mouth part of the filter bag (21) is fixedly connected to the round mouth of the flower plate (22), a plurality of round mouths are formed in the flower plate (22), and each round mouth is tightly connected with one filter bag (21).

3. The integrated treatment system for multiple pollution sources of coal gas according to claim 1, wherein the self-cleaning filter cylinder is used as a central annular distribution filter bag, the filter bag comprises a support frame and a filter bag outer bag, the cross sections of the support frame and the filter bag outer bag are elliptical or other shapes, the support frame is arranged in the filter bag outer bag for supporting the filter bag outer bag, and the support frame and the filter bag outer bag are matched in size.

4. The integrated coal gas multi-pollution source treatment system of claim 1, wherein the reverse pressurized ash removal zone (171) comprises a reverse dosing ash removal zone comprising a nozzle (1711), a rotary blowing arm (1712), a rotary blowing pipe (1713), a sealing portion (1714), a motor and gear drive (1715), a blowing drum (1716), a pulse valve (1717); the nozzles (1711) are disposed along the rotary blowing arm (1712).

5. The integrated abatement system of multiple pollution sources for coal gas according to claim 1, wherein the reverse pressurized deashing zone (171) employs a rotating double arm reverse pressurized deashing and is organically combined with the dry dedusting and desalting zone (172).

6. The integrated coal gas multi-pollution source treatment system of claim 1, wherein the pressure atomization zone (173) comprises a dosing tank (1731), a dosing pump (1732), a temperature control system (1733), and an atomizer (1734), the dosing tank (1731) being connected to the atomizer (1734) sequentially via the dosing pump (1732) and the temperature control system (1733).

7. The integrated coal gas multi-pollution source treatment system according to claim 1, wherein in the pressure atomization zone, the chemical stored in the chemical tank (1731) is subjected to chemical-adding atomization through a chemical-adding pump (1732) and an atomization nozzle (1734), the atomization pressure is between 3bar and 4bar, and the flow rate of the chemical-adding spray is controlled through a temperature control system (1733).

8. The coal gas multi-pollution source integrated treatment system of claim 1, wherein the pressure atomization zone (173) further comprises a gas distribution plate (1735), the gas distribution plate (1735) being disposed in a lower portion of the atomizer; the atomizing nozzle (1734) is provided at an upper portion of the gas distribution plate and a lower portion of the filter bag (21).

9. The integrated coal gas multi-pollution source treatment system according to claim 1, wherein the reverse pressurization ash removal area (171), the dry dedusting and desalting area (172), the pressure atomization area (173) and the ash storage and discharge area (174) are integrated in a cone container; the uppermost part is a reverse pressurizing ash removing area (171), and the next lower part is a dry dedusting and desalting area (172); the middle part is a pressure atomization area (173), and the lowest part is an ash storage and discharge area (174).

10. The integrated abatement system of claim 1, wherein the reverse pressurized ash removal zone (171) employs a multi-stage motor gear drive such that the rotational speed of the rotating double or multiple arms is less than 5 rpm.

11. The integrated treatment system for multiple pollution sources of coal gas according to claim 10, wherein the raw gas is discharged from a normal-low pressure gasification device (11), and the raw gas enters a heat exchanger (13) for waste heat recovery after large-particle materials are removed by a primary gas-solid separation device (12); the crude gas after heat exchange enters a self-cleaning filter (17) to become clean gas, and then enters a gas washing tower (14) to further cool the gas and enter a later-stage flow.

12. The utility model provides a normal, many pollution sources of low pressure coal gas integration treatment system, its includes normal pressure gasification process, cyclone, waste heat recovery process, washing separation process and cooling recovery process, its characterized in that: a washing and separating process consisting of a self-cleaning filter (17) and an ash bin (45) and a cooling and recovering process consisting of a direct cooling tower (46) and a cooling tower (48) which are respectively communicated with the waste heat boiler (43) and the self-cleaning filter (17) are arranged after the waste heat recovering process; thus forming an integrated treatment system for multiple pollution sources of normal and low pressure coal gas;

The inlet of the self-cleaning filter (17) is connected with the hot gas outlet of the waste heat boiler (43) to obtain a high-temperature waste heat gas source cooled by the waste heat boiler, the upper outlet of the self-cleaning filter (17) is connected with the direct cooling tower (46) in the cooling recovery procedure, the lower outlet of the self-cleaning filter (17) is connected with the ash bin (45) through a conveyer (49) to realize the conveying of waste in the self-cleaning process, and the ash bin (45) discharges accumulated ash together with ash generated in the upstream procedure through a conveying pipeline;

the self-cleaning filter comprises a reverse pressurizing and ash removing area (171), a dry dedusting and desalting area (172), a pressure atomizing area (173) and an ash storing and discharging area (174), wherein the reverse pressurizing and ash removing area (171) reversely pressurizes air to reversely blow the filter bag through rotating the double arms, so that dust, glue and salt adsorbed outside the filter bag are shaken off by vibration; the dry dedusting and desalting area (172) physically filters dust, glue and salt in the gas through a filter bag and a filter membrane which are arranged in a circumferential way; the pressure atomization area (173) regulates the temperature and captures aerosol through atomized medicament and water so as to promote and realize the growth of aerosol droplets, and is matched with physical filtration to remove glue and tar; the ash storage and discharge area (174) is used for storing ash, glue and salt and controlling the ash, glue and salt discharge; the pressure atomization area is a pressure atomization semi-dry tar removal area; the gas washing water in the gas washing tower is circularly used after being subjected to airtight cooling through a water heat exchanger; the increment washing water is recycled to the jacket and the heat exchanger of the normal low pressure gasification device after being softened and changed into steam to be recycled to the normal low pressure gasification device;