CN110734786A

CN110734786A - self-cleaning filter

Info

Publication number: CN110734786A
Application number: CN201910898570.XA
Authority: CN
Inventors: 周列
Original assignee: Shanghai Environmental Protection Energy Polytron Technologies Inc
Current assignee: Shanghai Environmental Protection Energy Polytron Technologies Inc
Priority date: 2018-11-22
Filing date: 2019-09-23
Publication date: 2020-01-31
Anticipated expiration: 2039-09-23
Also published as: CN110734785B; CN110734786B; CN110734785A

Abstract

The invention provides self-cleaning filters, which comprise a reverse pressurizing ash cleaning area, a dry dedusting and desalting area, a pressure atomization area and an ash storage and discharge area, wherein the reverse pressurizing ash cleaning area enables dust, glue and salt adsorbed outside a filter bag to vibrate and shake off by reversely pressurizing gas and reversely blowing the filter bag through rotating double arms, the dry dedusting and desalting area is provided with the filter bag and the filter membrane in the annular direction to physically filter the dust, glue and salt in the gas, and the pressure atomization area regulates the temperature and catches aerosol through atomizing medicaments and water to promote and realize gas and aerosol captureThe sol droplets grow up, and are matched with physical filtration to remove glue and tar, and the ash storage and ash discharge area is used for storing ash, glue and salt and controlling the discharge of ash, glue and salt. The invention adopts the rotary double-arm reverse pressurizing recoil ash removal technology and combines the high-efficiency nozzle, and the single-tank gas treatment capacity can reach 45000Nm³The invention has more compact integral structure and greatly reduces transmission parts and instrument configuration.

Description

self-cleaning filter

Technical Field

The invention relates to the technical field of industrial coal gas production, in particular to self-cleaning filters which are suitable for efficiently filtering substances such as dust, glue, salt and the like in a normal-pressure and low-pressure coal gas production system.

Background

In the coal gas industry of China, the normal and low pressure coal gas making process accounts for more than 60% of the whole gas making process. The process has the obvious advantages of simple gas making process, low investment and the like, but has the obvious disadvantages, particularly has great environmental protection pressure, and mainly shows that a large amount of water slag, wastewater which is difficult to treat and has extremely high treatment cost and serious aerosol emission cause great harm to the environment and posts, and the process can be eliminated if not fundamentally changed.

The current domestic commonly-used normal-low pressure gas making process flow (as shown in figure 1) basically comprises the following steps: five process flows of normal pressure gasification, cyclone separation, waste heat recovery, washing separation and cooling recovery.

Raw coke oven gas component, which is the raw coke oven gas produced by incomplete combustion of carbon in the raw coke oven gas under the combined action of oxygen (air, oxygen-enriched oxygen and pure oxygen) and water vapor within the temperature range of ,

C+O₂→CO

C+H₂O→H₂+CO

its combustion products mainly include CO and H₂、CH₄The effective components and phenol and H which are simultaneously associated₂S、HCN、NH₄Etc. and a large amount of solid particles.

The current stage is the main treatment process (as shown in figure 1): high-temperature raw gas enters a waste boiler process for heat exchange after large particles are removed by cyclone dust removal, low-pressure steam is generated as a byproduct, the exhaust temperature after the treatment of the waste boiler is usually 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 line-blowing filter bag and blowing tube set up as shown in FIG. 2 is generally used, which is a single tank 12000Nm³The device comprises a blowing pipe, wherein a pulse valve 3001 for controlling on-off is arranged on a blowing pipe pipeline 3002, the blowing pipe pipeline 3002 is connected to filter bags 3003, a nozzle is correspondingly arranged at the position of about 100mm (millimeter) above the opening of each filter bag 3003, the nozzle is fixedly connected to the blowing pipe, the pulse valve 3001 is switched on and off intermittently, so that a back-blowing airflow can be finally ejected through the nozzle by the blowing pipe according to requirements, and the airflow pulse generated by ejection enables the filter bag 3003 to expand and drop ash outside the filter bag. The system shown in figure 2 has the technical defects of large filtering area, too many pulse valves and nozzles and large occupied area.

In addition, because the environmental protection of the production enterprises is improved by 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 high: the waste water after washing contains a large amount of particles and a large amount of coal tar and ammonia nitrogen components, so that the waste liquid is difficult to treat to reach the discharge standard by an effective economic means;

2) the circulating cooling water has large amount of cooling water, high impurity content and corrosive components, high aerosol generation amount of high-volatility organic matters, high toxicity of the high-volatility organic matters, great harm to the environment and occupational health and the high-volatility organic matters which are also main components forming PM 2.5;

3) because of the existence of a large amount of waste water and waste residues, the environmental-friendly production in a factory is difficult to guarantee, particularly, harmful substances such as sewage ammonia nitrogen and the like are inevitably discharged every time when rainwater exists, the water quality is seriously influenced, and underground water and soil pollution 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 self-cleaning filters which are suitable for efficiently filtering substances such as dust, glue, salt and the like in a normal-pressure and low-pressure coal gas system.

According to the technical scheme, the self-cleaning filters are provided and comprise a reverse pressurizing ash removal area, a dry dedusting and desalting area, a pressure atomization area and an ash storage and discharge area, wherein the reverse pressurizing ash removal area enables dust, glue and salt adsorbed outside a filter bag to vibrate and shake off by reversely pressurizing gas through rotating double arms to reversely blow the filter bag, the dry dedusting and desalting area physically filters the dust, glue and salt in the gas through the filter bag and the filter membrane which are arranged annularly, the pressure atomization area adjusts the temperature and catches the aerosol through atomizing medicaments and water to promote and realize the growth of aerosol droplets and remove the glue and tar through physical filtration, the ash storage and discharge area is used for storing the ash, the glue and the salt and controlling the discharge of the ash and the glue and the salt, and the pressure atomization area is preferably a pressure atomization semi-dry tar removal area.

The dust storage and removal area is in a cone shape and is connected with a self-cleaning filter cylinder, a nitrogen cannon is arranged on the side wall of the cone of the dust storage and removal area, a feeding level meter, a storage temperature measuring device and a discharging level meter are preferably arranged on the side wall of the cone opposite to the nitrogen cannon from top to bottom, the feeding level meter is used for monitoring the upper limit of stored dust, when the stored dust is detected to reach the upper limit of a high level, the feeding level meter can send a dust removal starting signal to the self-cleaning filter in the form of digital display or vibration signals or sound alarms, when the stored dust layer is detected to reach the feeding level, a lower valve is opened to discharge the dust, when the stored dust layer is detected to reach the discharging level, the lower valve is closed to continue storing the dust, the nitrogen cannon arranged on the side wall of the dust storage and removal area vibrates to remove the dust accumulated on the side wall of the dust storage and the dust removal area through a cloth bag, a plurality of circular filter bags are fixedly connected to the circular opening of the pattern board, and a plurality of circular filter bags are tightly connected through a plurality of circular filter bags .

The self-cleaning filter is characterized in that a reverse pressurizing ash cleaning area 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 nozzle is arranged along the rotary blowing arm, the reverse pressurizing ash cleaning area adopts rotary double-arm reverse pressurizing ash cleaning as a characteristic and is organically combined with a dry dedusting and desalting area to achieve the maximum ash cleaning effect by using the minimum capacity, the pressure atomization area comprises a dosing tank, a dosing pump, a temperature control system and an atomization nozzle, the dosing tank is sequentially connected with the atomization nozzle through the dosing pump and the temperature control system, and the dosing pump and the atomization nozzle are used for dosing the medicament stored in the dosing in the pressure atomization area, the dosing pressure is between 3bar and 4bar, and the flow rate is controlled by the atomization system.

Preferably, the pressure atomizing area further comprises a gas distribution plate disposed below the atomizing nozzle, and the atomizing nozzle is disposed above the gas distribution plate and below the filter bag.

The reverse pressurizing ash cleaning area, the dry dedusting and desalting area, the pressure atomizing area and the ash storing and discharging area are integrated in conic containers, the reverse pressurizing ash cleaning area is arranged at the uppermost part, the dry dedusting and desalting area is arranged next to the lower part, the pressure atomizing area is arranged next to the lower part, and the ash storing and discharging area is arranged finally.

In the second technical scheme of the invention, a integrated treatment system of coal gas multiple pollution sources is provided, which comprises a normal-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 normal-low pressure gasification device, the primary gas-solid separation device, the heat exchanger, the self-cleaning filter, the gas washing tower and a pressure atomization zone of the water heat exchanger are sequentially connected, the pressure atomization zone of the primary gas-solid separation device is used as a subsequent treatment device of the normal-low pressure gasification device, the heat exchanger is used as a subsequent treatment device of the pressure atomization zone 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.

In the coal gas multi-pollution source gasification treatment system, raw coal gas is discharged from a normal-low pressure gasification device, large-particle materials are removed by a pressure atomization zone of a primary-effect gas-solid separation device, then the raw coal gas enters a heat exchanger for waste heat recovery, the raw coal gas after heat exchange enters a self-cleaning filter to become clean coal gas, then enters a gas washing tower to enter , the temperature of the gas is reduced, the gas is cooled to become clean coal gas with the temperature lower than 50 ℃.

In the coal gas multi-pollution source integrated treatment system, a 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 atomization area at the middle lower part and a reverse pressurization ash cleaning area at the upper part, wherein the ash storage area is used for storing filtered dust, the dust is accumulated to a fixed material position and then is discharged downwards through a dry residue outlet, an atomization nozzle is arranged at the top of the pressure atomization area, a dosing tank, a dosing pump and a temperature control system are arranged outside the pressure atomization area, the dosing tank is sequentially connected with the dosing pump, the temperature control system and the atomization nozzle, and the pressure atomization area is used for removing tar and aerosol.

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

In the third technical scheme, the invention provides kinds of normal and low pressure coal gas multi-pollution source integrated treatment systems, which comprise four working procedures of normal pressure gasification, cyclone separation, waste heat recovery, washing separation and cooling recovery, wherein sets of washing separation working procedures consisting of self-cleaning filters and ash bins and waste heat boilers respectively are additionally arranged after the waste heat recovery working procedure.

Preferably, an inlet of the self-cleaning filter is connected with a hot gas outlet of the waste heat boiler to obtain a high-temperature gas source of waste heat cooled by the waste heat boiler, an outlet at the upper part of the self-cleaning filter is connected with a direct cooling tower in a cooling and recycling process, an outlet at the lower part of the self-cleaning filter is connected with an ash bin through an conveyor to realize the conveying of waste in the self-cleaning process, the ash bin discharges accumulated ash and slag generated in an upstream process through a conveying pipeline, and the inlet step is carried out.

Compared with the prior art, compared with the prior bag-type dust remover which adopts inert gas for pulse back blowing, groups (standard dry) gas volume of 45000Nm³Bag-type dust collector for/h coal gas productionIn 4 single tanks and above, the invention adopts the rotary double-arm reverse pressurization backflushing ash removal technology and combines a high-efficiency nozzle, and the single-tank treatment (standard dry) gas amount can reach 45000Nm³The invention has more compact integral structure and greatly reduces the arrangement of moving parts and instruments.

For 45000Nm³The number of pulse valves adopted by the invention is 1-2, the total number of nozzles is greatly reduced to 20-30, and pulse valves are required to be arranged in each rows for the existing row injection, for 45000Nm³The coal gas production per hour needs at least 4 tanks, the total number of pulse valves is more than 32, and the number of nozzles is more than 448. The capacity of single tank for processing raw coke oven gas reaches 45000Nm³H and above (usually the single-tank processing capacity of the cloth bag dust removal of coal gas is usually less than 15000Nm³/h)。

Drawings

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

FIG. 2 is a schematic diagram of a conventional filter bag and blowing tube arrangement for blowing;

FIG. 3 is a schematic structural view of a 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 diagram of the nitrogen cannon of FIG. 4;

FIG. 6 is a schematic diagram of the pressure atomization zone of FIG. 3;

FIG. 7 is a schematic structural view of the pressure atomizing nozzle of FIG. 6;

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

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

FIG. 10 is a connection structure of the cloth bag and the card 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 view 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 the pulse valve of FIG. 12;

FIG. 15 is a schematic view of the motor and gear assembly of FIG. 12;

FIG. 16 is a diagram of the steps for using the self cleaning filter of the present invention;

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

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

FIG. 19 is a schematic diagram of an integration treatment process using the coal gas multiple pollution source of the present invention;

FIG. 20 is a schematic structural diagram of the normal-low pressure gasification device shown in FIG. 19;

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

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

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

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

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

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

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

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

fig. 29 is a schematic diagram of a coal gas multi-pollution source integrated treatment process adopting a two-stage scrubber process.

FIG. 30 is a schematic diagram of a fourth embodiment of a coal to gas multi-pollution source integrated abatement system in accordance with the present invention;

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

Detailed Description

The invention is further illustrated at in conjunction with the drawings and embodiments of the invention are presented.

The self-cleaning filter can be applied to a normal and low pressure coal gas making system, and has the main effects that particulate matters, salt and coal tar in raw gas are removed by physical filtration, solid particulate matters using the self-cleaning filter can be removed by more than or equal to 99.99%, and the tar removal rate is more than or equal to 90%, and the raw gas is changed into clean gas after passing through the self-cleaning filter.

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 ash removal area 171, a dry dedusting and desalting area 172, a pressure atomization area 173 and an ash storage and discharge area 174, wherein the reverse pressurizing ash removal area 171 reversely blows back the filter bag by rotating a double-arm reverse pressurizing gas, so that the dust adhesive adsorbed outside the filter bag vibrates and shakes off; the dry dedusting and desalting zone 172 physically filters dust and colloidal salt in the gas through a filter bag and a filter membrane which are annularly arranged; the pressure atomization region 173 adjusts the temperature and captures the aerosol by 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 discharge area 174 is used for storing ash gum and salt and controlling the discharge of ash gum and salt.

FIG. 4 is a schematic view showing the structure of the ash storage and discharge area 174 of FIG. 3, wherein the ash storage and discharge area 174 has a cone shape, the cone-shaped ash storage and discharge area is connected to a self-cleaning filter cylinder for storing ash (tar, salt) and discharging ash, the lower valve is opened to discharge ash when the stored ash layer is detected to reach a loading position, the lower valve is closed to continue ash storage when the stored ash layer is detected to reach a discharging position, the nitrogen cannon 1744 provided on the side wall of the cone of the ash storage and discharge area vibrates the ash accumulated on the side wall of the cone by the vibration generated by the instantaneous release of nitrogen released by the pulse at a high speed, the nitrogen cannon 1744 is provided on the side wall of the cone , the loading level meter 1741, the storage temperature measuring device 1742, and the discharging level meter 1743 are preferably provided on the side wall of the cone opposite to the nitrogen cannon 1744 from the top to the bottom, and in addition, the loading level meter 1741, the storage temperature measuring device 1742, and the discharging level meter 1743 may be provided at appropriate positions.

The material loading level indicator 1741 is used for monitoring the upper limit of ash storage, and when detecting that the ash storage reaches the upper limit of high material level, the material loading level indicator 1741 can send an ash discharge starting signal to the self-cleaning filter in the forms of digital display, vibration signal or sound alarm and the like. The material discharge level indicator 1743 is used for monitoring the lower limit of ash storage, and when detecting that the ash storage reaches the lower limit of low material level, the material discharge level indicator 1743 can send an ash discharge end signal to the self-cleaning filter in the forms of digital display, vibration signal or sound alarm, etc. The storage temperature measuring device 1742 is used to detect the temperature or/and moisture of the ash storage and discharge area. The nitrogen cannon 1744 is used for pulse vibration of the ash storage and discharge area to prevent material caking.

Fig. 5 is a schematic structural diagram of the nitrogen cannon 1744 in fig. 4, the nitrogen cannon 1744 includes a nitrogen bag 441, a pulse valve 442 and a pipeline system 443, the nitrogen bag 441 is communicated with the pipeline system 443 through the pulse valve 442, the nitrogen bag 441 can be a high-pressure nitrogen bag, or can be a gas source connected to a high-pressure gas supply pipeline, and by opening and closing the pulse valve 442 in a pulse timing manner, gas in the nitrogen bag 441 enters the ash storage and discharge area 174 in a cone shape through the pipeline system 443 at a high speed, so as to form a pulse high-speed gas impact on the bin wall 444, so that the bin wall 444 generates pulse vibration, and further prevents material from caking.

Fig. 6 is a schematic structural diagram of the pressure atomizing area 173 in fig. 3, the pressure atomizing area 173 includes a dosing tank 1731, a dosing pump 1732, a temperature control system 1733 and an atomizing nozzle 1734, the dosing tank 1731 is connected with the atomizing nozzle 1734 through the dosing pump 1732 and the atomizing nozzle 1734 in sequence, in the pressure atomizing area, the dosing pump 1732 and the atomizing nozzle 1734 are used for dosing and atomizing the medicament stored in the dosing tank 1731, the atomizing pressure is 3bar to 4bar in , the flow rate of the dosing spray is controlled through the temperature control system 1733, the temperature of the atomized medicament is controlled to capture the aerosol and tar, the pressure atomizing area 173 further includes a gas distribution plate 1735 arranged at the lower part of the atomizing nozzle 1735 for cutting the whole gas flow into small gas flows to prevent the turbulent flow, the atomizing nozzle 1734 is arranged at the upper part of the gas distribution plate, the lower part of the filter bag 21 mainly functions to atomize the tar and capture the aerosol and tar, and the atomizing nozzle 1734 is preferably a pressure atomizing nozzle 1734.

FIG. 7 is a schematic view showing the arrangement structure of the pressure atomizing nozzles 1734 in FIG. 6. in the pressure atomizing area 173 of the self-cleaning filter, the pressure atomizing nozzles are uniformly distributed on the half circumference of the side housing of the self-cleaning filter, and are installed in the self-cleaning filter cylinder through connecting flange pipes, so that the atomization is uniform and the atomization radius is large, thereby achieving the purpose of fully capturing aerosol and tar.

Fig. 8 is a schematic structural view of the gas distribution plate of fig. 6, which is configured to divide the circumference into a plurality of sections by the horizontal partition plates 201 and the vertical partition plates 202, cut the gas flow into small gas flow distribution, prevent turbulence, and improve the filtering efficiency.

FIG. 9 is a schematic structural diagram of the dry dedusting and desalting zone in FIG. 3, the dry dedusting and desalting zone completes dedusting and desalting by using a cloth bag, the mouth of the filter bag 21 is fixedly connected to the circular mouth of the faceplate 22, the faceplate 22 is provided with a plurality of circular mouths, each circular mouths are tightly connected with filter bags 21, and dust and glue salt are filtered when the air flow passes through the filter bags.

FIG. 10 is a connection structure of the cloth bag and the card shown in FIG. 9, FIG. 11 is a schematic view of the arrangement of the cloth bag shown in FIG. 9, which changes the distribution of the original filter bags by blowing in a circular direction, so that the filter bags are more compactly distributed, more filter bags are arranged per unit area, and the filtering efficiency is higher than 40%.

As shown in fig. 10-11, the outer bag is a straight-through filter bag with an open upper end and a closed bottom end, and the straight-through filter bag is preferably a dust removal bag. The upper end opening of the filter bag outer bag comprises a concave ring-shaped clamping structure, namely a bag ring. When the mounting device is mounted, the pattern plate is clamped at the concave annular bag ring. The filter bag outer bag comprises a filter bag lower section. The fabric of the straight-through filter bag is made of a material which is efficient in filtering, easy in dust stripping and durable in use, and the straight-through filter bag is preferably an aramid fiber or polyester fiber dust removal cloth bag. In use, dust is attached to the outer surface of the outer bag of the filter bag. When the dust-containing gas passes through the filter bag, the dust is trapped on the outer surface of the filter bag, and the clean gas enters the interior of the filter bag through the filter material. Because the filter cloth is filtered by depending on the thickness of the whole filter layer and belongs to deep filtration, a three-dimensional loose porous structure is formed by fibers in the depth direction of the whole filter layer of the straight-through filter bag, and gradient filtration is formed from loose to compact from inside to outside, and the filter cloth has the advantages of high dirt capacity, long filter life, low pressure difference and the like.

, as shown in FIGS. 10-11, the card is clamped in the groove of the outer bag of the filter bag (clamping structure, i.e. bag ring), and the card is fixed under the clamping of the groove, the card is used to fix the filter bag as a whole, at this time, the outer layer of the outer bag of the filter bag is in contact with the card, and the inner layer of the outer bag of the filter bag is in contact with the support frame.

The filter bag and the flower plate are installed by lightly inserting the outer bag of the filter bag into the hole of the flower plate, grasping the outer bag opening of the filter bag, slowly feeding the outer bag of the filter bag into the flower plate until the outer bag body of the filter bag is naturally vertical, tightly holding the groove-shaped spring ring (groove (clamping structure, namely bag ring)) of the outer bag of the filter bag with two hands, bending the spring ring to form a C shape, holding the side of the embedded bulged C-shaped spring ring by , fixing the bulged C-shaped spring ring on the flower plate by handles, slowly stretching the other side of the spring ring of the outer bag of the filter bag, just embedding the groove of the spring ring into the inner side of the flower plate hole, slowly placing the support frame of the filter bag into the outer bag of the filter bag after the outer bag is installed, prohibiting the free falling body of the support frame of the filter bag from falling down to cause the flanging of the filter bag support frame to be damaged, and embedding the inner concentric ring layer and the outer concentric ring layer of the support frame on the opening.

, the filter bag is fixed to the top base of the tower through a clean room, the filter bag is fixed to the top base of the tower through a flower plate, the clean room is usually fixed to a fixed beam on the top of the urea prilling tower, the other end of the clean room is welded to the box of the dust collector in a sealing mode, the filter bag is fixed and positioned with the dust collecting box through the flower plate, the dust collecting box is divided into an upper layer and a lower layer by the flower plate, the upper layer of the flower plate is the clean room, the lower layer of the flower plate is the dust recovery room, the flower plate is provided with a plurality of openings, the filter bags are respectively and vertically arranged at the openings, the lower part of the dust collecting box is provided with an opening, the upper edge of the dust collecting box is arranged on the clean room, the induced draft fan is arranged above the clean room and comprises an air inlet and an air outlet, the air inlet of the induced draft fan is connected with the clean room through a pipeline, during dust collecting operation, the induced draft fan continuously extracts air in the clean room above the dust collecting box, the clean room, the air flows upwards along with the filter bag towards the filter bag, the.

Fig. 12 is a schematic structural diagram of the reverse pressurizing ash removal area in fig. 3, and the reverse dosing ash removal area includes a nozzle 1711, a rotary blowing arm 1712, a rotary blowing tube 1713, a sealing portion 1714, a motor and gear transmission mechanism 1715, a blowing steam drum 1716, a pulse valve 1717, and a rotary blowing arm reinforcing rib 1718. The nozzle 1711 is arranged along the rotary blowing arm 1712, in order to enhance the rigidity and strength of the blowing tube, a rotary blowing arm reinforcing rib 1718 is arranged on the rotary blowing arm 1712, and the rotary blowing arm reinforcing rib 1718 is arranged between the rotary blowing tube 1713 and the rotary blowing arm 1712 and plays a role in pulling and fixing; and the rotary blowing arms 1712 are uniformly arranged into 2-3 pieces, preferably 2 pieces along the radial direction of the inner diameter of the self-cleaning filter cylinder body, a plurality of nozzles 1711 are arranged at the lower side of the rotary blowing arms 1712, and the back blowing inert gas is uniformly blown in 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 in axisymmetric connection around the rotary blowing pipe 1713; a sealing portion 1714 is provided at the connection of the self-cleaning filter cartridge with the rotary blowing arm 1712 to improve the sealing of the self-cleaning filter cartridge. The upper end of the rotary blowing pipe 1713 is connected with a blowing steam drum 1716 through a pulse valve 1717. The motor and gear transmission mechanism 1715 drives the rotary blowing pipe 1713 and the rotary blowing double arms 1712 to rotate, and releases the pressurized inert gas in the blowing steam pocket 1716 to be sprayed out at high speed through the nozzle 1711 by opening the pulse valve 1717 at fixed time. The nozzles blow over the entire filter bag as the motor and gear drive 1715 is rotating. The reverse pressurized airflow impacts the lower filter bag and is transmitted to the bottom of the filter bag, so that ash (containing tar and salt) and the like adsorbed outside the filter bag fall off to an ash storage area. Wherein the sealing of the gas inside the apparatus from the outside is achieved by the sealing portion 1714.

Fig. 13 is a schematic view showing the connection of the nozzle of fig. 12 to the rotary blowing arm, in which the nozzle 1711 is disposed under the rotary blowing arm 1712, and the nozzle 1711 and the rotary blowing arm 1712 are connected by a bolt or a rivet.

FIG. 14 is a schematic illustration of the connection of the purge drum and the pulse valve of FIG. 12; the blowing steam pocket 1716 is used for storing a large amount of backflushing inert gas, is opened by matching with the pulse of the pulse valve 1717, and performs blowing on the upper part of the cloth bag through a nozzle by the middle rotary blowing arm 1712 and the rotary blowing pipe 1713, and finally realizes reverse pressurization pulse ash removal.

Fig. 15 is a schematic connection diagram of the motor and the gear transmission mechanism in fig. 12, wherein the motor 154 drives the bevel gear pair 153, the bevel gear pair 153 is engaged with the pinion 152, the pinion 152 is engaged with the bull gear 151, and the rotation speed of the rotary blowing arm 1712 is required to be achieved, wherein the rotation speed of the rotary blowing arm is less than 5 rpm.

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

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

secondly, atomizing and capturing aerosol and tar by a semi-dry method;

thirdly, removing dust and glue by a dry method;

fourthly, reversely pressurizing to remove ash and discharge ash.

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

, the raw gas enters into the self-cleaning filter through the raw gas inlet 4001, and the gas flow is cut into small gas flows through the gas distribution plate 4002

A second step; the crude gas is treated by atomization 4003 of semi-dry atomization medicament to capture aerosol and tar

A third step; the crude gas is then passed through a filter bag 4004 for dry dedusting and degumming (containing aerosol), and finally discharged from a clean gas outlet 4005

The fourth step; the dust and salt (including aerosol and glue oil) accumulated in the filter bag are blown by the reverse pressurizing ash removal 4006, and the dust glue falls into the dust storage bin and is discharged through the lower port.

Fig. 18 is a schematic view of applying the self-cleaning filter of the present invention to a normal and low pressure coal gas system, in which the self-cleaning filter 17 of the present invention is installed 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 through the self-cleaning filter, wherein the removal rate of ash is 99.99%, and the removal rate of aerosol and tar is 90%, the ash is removed, aerosol and aerosol oil are delivered to an ash silo, thereby purifying the raw gas, specifically, according to fig. 18, pipes 57 directly connected to the normal pressure gasification furnace 41 are installed on the main pipe of the cooling tower 48 communicating with the waste heat boiler 43, evaporators 58 are additionally installed in the branch pipe, and the incremental water containing oxygen, salt and oil removed and gum output from the cooling tower 48 is delivered to the normal pressure gasification furnace 1 after evaporation treatment, and the process of integration of the normal and low pressure coal gas multi-pollution source is provided:

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; under the cyclone separation action, mixed gas containing dust with smaller mass is guided into a waste heat boiler 43 through an output pipeline arranged at the upper part of a cyclone separator for cooling treatment, then the raw gas after cooling treatment enters an inner cavity of a shell of a 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 particles, salt and aerosol mixed in the raw gas are filtered through the filtering treatment of a filtering unit 55, the raw gas is connected to an input interface a of a direct cooling tower 46 through an outlet cut-off valve component 53 arranged at the upper part of the self-cleaning filter and a conveying pipeline connected with the outlet cut-off valve component 53, and water gas is formed after water cooling treatment in the direct cooling tower 46 and is conveyed to a subsequent process 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 interface E 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 particle impurities discharged by the self-cleaning filter 17 and 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 a waste material conveying main pipe 56 through the lower output pipeline of the ash bin for transportation;

C. when the A, B step is performed, two output ports H, I and input ports J are arranged on the lower furnace body of the waste heat boiler 43, the output port H is communicated with the inner cavity of the normal pressure gasification furnace 41 through an output pipeline, and the input port J of the waste heat boiler 43 is connected with a port G of the cooling tower 48 through a connecting pipeline;

D. while the step A, B, C is performed, the atmospheric gasifier 41, the cyclone 42, the waste heat boiler 43, and the ash silo 45 transport slag and ash having a calorific value generated during their operations to a waste collecting point through the waste discharge pipes, respectively, via the waste transport header 56.

In the treatment process, branch pipelines 57 directly connected to the normal pressure gasification furnace 41 are arranged on a main pipeline communicated to the waste heat boiler 43 by the cooling tower 48, evaporators 58 are additionally arranged in the branch pipelines, and the incremental water which is output by the cooling tower 48 and contains the removed oxygen, salt and oil glue is sent to the normal pressure gasification furnace 41 after being subjected to evaporation treatment, so that the problem that the excessive waste water is converted into steam by the evaporators 58 and then sent to the normal pressure gasification furnace 41 to participate in the gasification of lump coal under the condition that the cooling water accumulated by the cooling tower 48 is excessive is solved.

In addition, according to another technical scheme provided by the invention, the coal gas multi-pollution source integrated treatment system and method are provided by the invention, as shown in fig. 19, 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, crude gas is discharged from the normal-low pressure gasification device 11, 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, then enters the gas washing tower 14 to be cooled to become clean gas with the temperature lower than 50 ℃ and then enters a rear-stage process, washing water is cooled by the water heat exchanger 18 and then returns to the gas washing tower 14 for recycling, part of incremental washing water is returned to a jacket of the normal-low pressure gasification device 11 to become the steam return-normal-low pressure gasification device 11, and part of incremental washing water is returned to the normal-low pressure gasification device 11 and is discharged to a secondary boiler through the normal-low pressure gasification device 11 and the primary gas-solid separation device 12 and the dry ash mixing filter 17.

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

As shown in FIG. 20, the normal-low pressure gasification device 11 is used for gasifying lump coal, coal powder and the like into crude coal gas, and comprises a tank body, a jacket coaxial with the tank body is arranged outside the tank body, a th inlet 113 is arranged on the side surface (preferably arranged at the middle upper part) of the tank body, a second inlet 114 is arranged on the side surface (preferably arranged at the middle lower part) of the tank body, the second inlet 114 is positioned below or below the th inlet 113, a gasifying agent water vapor inlet 112 is also arranged on the side surface (preferably arranged at the middle lower part) of the tank body and penetrates through the jacket to enter the tank body, an incremental washing water inlet 117 and a jacket vapor outlet 115 are respectively arranged outside the jacket, and a th inlet 113 penetrates through the jacket to enter the tank body and is used for feeding materials such as lump coal, coal and the like into the tank body.

In the normal-low pressure gasification device 11, lump coal and pulverized coal enter the normal-low pressure gasification device from an inlet 113 of , air, oxygen-enriched air or pure oxygen enters from an inlet second inlet 114, water vapor of a gasifying agent enters from an inlet 112 of the water vapor of the gasifying agent, the raw coal gas is gasified under the action of the gasifying agent to form the raw coal gas and is discharged from a top raw coal gas outlet 111, slag is discharged from a bottom slag discharge port , part of the augmented water from the outlet of the gas washing tower enters an augmented water jacket from an inlet 117 and is changed into steam and is discharged for recycling from an outlet 115.

As shown in fig. 21, the primary gas-solid separation device 12 is used to separate large particle dust from the raw gas. The raw gas enters the primary gas-solid separation device from the tangent line of the raw gas inlet 122, under the dual actions of centrifugal force and gravity, large particles contained in the raw gas settle in the gas-solid separation device 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 is used to cool the raw gas to a temperature of 140-240 ℃. The incremental washing water is changed into water vapor through heat exchange, and then the water vapor is returned to the normal-low pressure gasification device 11 to be used as a gasification agent, and enters from the inlet 112 for use. High-temperature crude gas enters the heat exchanger from the crude gas inlet 131, is discharged from the crude gas outlet 134 after being subjected to sufficient heat exchange with water in the heat exchanger, the temperature is reduced to between 140 ℃ and 220 ℃, incremental washing water enters the heat exchanger from the inlet 133 and is changed into steam after heat exchange with the crude 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 gasification agent.

The self-cleaning filter 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 173 (preferably a pressure atomization semi-dry tar removing area) at the middle lower part and a reverse pressurization ash removing area 171 at the upper part, wherein the ash storage area 174 is used for storing filtered dust, the dust is deposited to and then is discharged downwards through a dry residue outlet 17c, an atomization nozzle 1734 is arranged at the top of the pressure atomization area 173, a medicine feeding box 1731, a medicine feeding pump 1732 and a temperature control system 1733 are arranged outside the pressure atomization area 173, the medicine feeding box 1731 is sequentially connected with the medicine feeding pump 1732, the temperature control system 1733 and the atomization nozzle 1734, and the pressure atomization area 173 is used for removing tar and aerosol, wherein the flue gas temperature is locally controlled within a temperature range suitable for trapping aerosol by according to proportion, and simultaneously, a sufficient amount of fine suspended liquid drop trapping gas, tar and the like are generated.

The dry dedusting and desalting zone 172 is used for removing dust and salt, and it uses physical filtration principle to collect particulate matter (dust) and form dust layer with certain thickness on the surface layer, and uses porous dust adsorption to collect aerosol and fine droplets, the reverse pressurized dedusting zone 171 removes ash by pressurization, which uses reverse pressure to shake off porous dust.

, the crude gas after passing through the heat exchanger, the temperature of which is between 140 and 240 ℃, enters from the crude gas inlet 17A at the side of the pressure atomization zone (near the bottom 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 ash cleaning zone 171, and is discharged from the clean gas outlet 17B arranged near the top side of the reverse pressurizing ash cleaning zone 171 to become clean gas, 99.9% of dust, more than 90% of aerosol and tar contained in the crude gas fall into the ash storage zone 174 under reverse pressurization, and then is discharged from the dry slag outlet 17C.

The self-cleaning filter has the main effects that particles, salt and coal tar in raw gas are removed by physical filtration, solid particles in the raw gas can be removed by more than or equal to 99.99 percent by using the self-cleaning filter, and the raw gas is changed into clean gas after passing through the self-cleaning filter, and the self-cleaning filter has the technical advantages that a dry dust removal and salt removal area 172, a pressure atomization area 173, a reverse pressurization ash removal area 171 and an ash storage area 174 are organically combined into , so that the solid particles can be removed by more than or equal to 99.99 percent, and the tar removal rate is more than or equal to 90 percent, in addition, a pressure atomization semi-dry tar removal technology is utilized in the pressure atomization area 173, so that a dosing tank 1731, a dosing pump 1732, a temperature control system 1733 and an atomization nozzle 1734 are organically combined, the automatic control of the temperature of the smoke is realized, and the control of atomization liquid is configured, so that the removal rate of micron and submicron aerosol and tar in the smoke reaches more.

Compared with the traditional bag-type dust remover which adopts pulse back blowing of inert gas, groups (standard dry) gas quantity of 45000Nm³The bag-type dust collector for coal gas production is usually arranged in 4 single tanks or more, the invention can adopt steps of reverse pressurizing and back flushing ash removal technology by rotating double arms and combining with high-efficiency nozzles, the gas quantity for single tank treatment (standard dry) can reach 45000Nm³The invention has more compact integral structure, greatly reduces the arrangement of moving parts and instruments, and has more stable and safe device. The single-tank crude gas treatment capacity of the invention reaches 40000Nm³H and above (usually the single-tank processing capacity of the gas bag dust removal is usually less than 15000Nm³/h)。

As shown in FIG. 24, the scrubber tower 14 is used for washing and cooling the clean gas to below 50 ℃ by using the washing water, and meets the requirements of the next process, the scrubber tower 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 tank body of the scrubber tower, the clean gas inlet 141 is arranged at the bottom of the main tank body of the scrubber tower, the clean gas outlet 142 is arranged at the top of the main tank body of the scrubber tower, the washing water inlet 143 is arranged at the side surface of the upper middle part of the main tank body of the scrubber tower, the washing water outlet 144 is arranged at the bottom of the main tank body of the scrubber tower, the washing water outlet 144 is arranged at a level slightly lower than the clean gas inlet 141, an atomizing device is arranged in the main tank body of the scrubber tower, the atomizing device is connected with the washing water inlet 143 and is used for atomizing the washing water, and.

Preferably, the 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 the reverse heat exchange of the 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 become high-temperature washing water after heat exchange/washing/cooling are completed and are discharged from the outlet 144.

As shown in fig. 25, the water heat exchanger is connected to the high temperature washing water of the scrubber from the outlet 144, and the water heat exchanger is used to cool the high temperature washing water in a closed cycle and recycle it. 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 and then is discharged from the washing water upper outlet 182, and then is recycled for spraying; the cooling water enters from the cooling water bottom inlet 184 and is discharged from the cooling water top outlet 183.

, as shown in FIG. 26, a steam storage tank is added on the basis of the coal gas multi-pollution source integrated treatment system of the invention, in the coal gas multi-pollution source integrated treatment system, lump coal and pulverized coal are fed into the normal-low pressure gasification device 11 through an inlet 113 through a coal feeding device, air, oxygen-rich gas or pure oxygen is fed from a bottom 114 through a blower through a connector, gasification agent steam is fed from an inlet 112, crude coal gas formed by gasification under the action of the gasification agent is discharged from a top 111, and slag is discharged from a bottom 116.

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

The 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 the reverse heat exchange of the atomized washing water; the washing water enters from the washing water inlet 143 through the pressure atomization nozzle, and becomes high-temperature washing water after the heat exchange/washing/cooling of the high-temperature clean gas is completed, and then is discharged from the outlet 144.

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 and then is discharged from the washing water upper outlet 182, and then is recycled for spraying. The cooling water enters from the cooling water bottom inlet 184 and is discharged from the cooling water top outlet 183.

Compared with the existing separation mode, 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 combined use of the self-cleaning filter and the gas washing tower not only reduces the pollution to the environment, but also reduces the occupied area and saves the equipment expenditure, thereby greatly improving the quality and the efficiency.

In yet another aspect of the present invention, alternative processes are provided, in which a dividing wall type cooler 24A is used to replace the scrubber 14 and the 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, after large particles are removed by the primary gas-solid separation device 12, 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 dividing wall type cooler 24A to cool the gas, the clean gas with the temperature lower than 50 ℃ enters the post-stage process, part of condensed water is recycled to the jacket of the normal-low pressure gasification device 11 to become steam and recycled to the normal-low pressure gasification device 11, and part of condensed water heat exchanger 13 to become steam and recycled to the normal-low pressure gasification device 11, and 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-.

As shown in the dividing wall cooler 24A of fig. 28, the dividing wall cooler 24A cools the clean gas to below 50 degrees celsius by means of dividing wall cooling (tubular heat exchanger, plate heat exchanger, etc.), and meets the requirements of the next process. The clean gas passing through the self-cleaning filter 17 enters from a clean gas inlet 24A3 of the dividing wall type cooler 24A, and is discharged from a clean gas outlet 24A4 after being cooled by the dividing wall type cooler 24A; the cooling water enters from the washing water inlet 24A1, the cooling water is discharged from the cooling water outlet 24A2, and the condensed water in the clean coal gas is discharged from 24A 5.

The dividing wall cooling process has greater technical advantages, firstly, condensed water in the clean gas is condensed by the dividing wall cooler and then recycled, so that the condensed water is prevented from being mixed with other water and is completely isolated from the atmosphere; and after the self-cleaning filter is additionally arranged, condensed water in the dividing wall type condenser only contains trace particles, organic matters and water-soluble gas and almost does not contain salt, the quality of washing water is close to the level of soft water, the washing water can return to a jacket of the normal-low pressure gasification device, and the washing water and the heat exchanger are changed into water vapor and then are recycled to the normal-low pressure gasification device as a gasification agent, so that the times and the efficiency of material recycling are improved.

Further , in the coal gas multiple pollution source gasification treatment system and method, a two-stage gas scrubber process (as shown in fig. 29) is adopted, raw gas is discharged from a normal-low pressure gasification device 11, large particles are removed by a primary gas-solid separation device 12 and then enters a heat exchanger 13 for waste heat recovery, the heat-exchanged raw gas enters a self-cleaning filter 17 to be changed into clean gas, then enters a th stage gas scrubber 34B to cool the clean gas to within 5 ℃ above the dew point temperature of the clean gas and then enters a second stage gas scrubber 34C, part of high-temperature washing water generated in the process enters a 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, part of high-temperature washing water enters a heat exchanger 13 to be changed into steam to be recycled to the normal-low pressure gasification device, the clean gas cooled by the th stage gas scrubber 34B passes through the second stage gas scrubber 34C to be cooled to the temperature required by the process, ℃ is discharged from the normal-low pressure gas scrubber 11, the primary gas-solid separation device 12, the primary gas scrubber 13 and the secondary gas scrubber 17 to be conveyed to the secondary ash self-cleaning filter 17.

The water inlet amount of an th-level scrubber can be quantitatively controlled by adopting the two-level scrubber, the water outlet temperature of the lower part of the scrubber is the highest after the purified gas is cooled to be within 5 ℃ above the dew point temperature of the purified gas, the water outlet amount of the lower part of the scrubber is ensured to be balanced with the water inlet amounts of a jacket of the normal-low pressure gasification device and a heat exchanger, the washing water entering the jacket of the normal-low pressure gasification device and the heat exchanger is ensured to be the highest by steps, and the energy is saved.

Further embodiments of the present invention will be described in detail with reference to the embodiments shown in fig. 30-31, wherein fig. 30 is a schematic diagram of a fourth embodiment of the coal gas multiple pollution source integrated abatement system according to the present invention, and fig. 31 is a schematic diagram of a self-cleaning filter employed in the system shown in fig. 30.

Referring to fig. 30 and 31, the treatment system integrated with the normal and low pressure coal gas multiple pollution sources comprises four steps of normal pressure gasification, cyclone separation, waste heat recovery, washing separation and cooling recovery, wherein sets of washing separation steps consisting of a self-cleaning filter 17 and an ash bin 45 and cooling recovery steps consisting of a straight cooling tower 46 and a cooling tower 48 which are respectively communicated with a waste heat boiler 43 and the self-cleaning filter 17 are additionally arranged after the waste heat recovery step, thereby forming the treatment system integrated with the normal and low pressure coal gas multiple pollution sources without pollution leakage.

The inlet of the self-cleaning filter 17 is connected with the hot gas outlet of the waste heat boiler 43 to obtain a waste heat high-temperature gas source cooled by the waste heat boiler, the outlet at the upper part of the self-cleaning filter 17 is connected with a direct cooling tower 46 in the cooling and recycling process, the outlet at the lower part of the self-cleaning filter 17 is connected with an ash bin 45 through an conveyor 49 to realize the conveying of waste in the self-cleaning process, and the ash bin 45 discharges accumulated ash residues with the ash residues generated in the upstream process 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 output port at the upper part of the self-cleaning filter, an output interface b at the upper part of the direct cooling tower 46 is directly connected with a coal gas output port and goes to the working procedure, the cooling tower 48 is provided with three interfaces, an output interface F is connected with an input interface c on the direct cooling tower 46 through an control pump 47, an interface E of the cooling tower 48 is connected with an output interface d at the lower part of the direct cooling tower 46, so that a closed cooling loop between the direct cooling tower 46 and the cooling tower 48 is formed, and meanwhile, another interface G of the cooling tower 48 is connected with the waste heat boiler 43.

The self-cleaning filter 17 comprises a shell 59, a sensing detection control unit 50, a pressure atomization unit 51, an inlet stop valve assembly 52, an outlet stop valve assembly 53 backwashing backflushing unit 54 and an overflowing unit 55, wherein the overflowing unit 55 is arranged on the middle upper part of the self-cleaning filter and plays a role in filtering from bottom to top.

Practical use shows that the normal and low pressure coal gas multiple pollution source integrated treatment system provided according to the technical scheme has the advantages that almost totally closed process flows are formed by a plurality of independent devices of a complete set of equipment for manufacturing water gas, so that closed process rings can be formed by sewage, ash, waste gas and the like which may appear in each process flows, 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 equipment is completely and effectively solved, and the system has great positive significance for the protection of production environment and even urban environment.

In view of the above, it is desirable to,the system and the process of the invention fundamentally change the components of the clean gas treated by the self-cleaning filter, and the components mainly comprise CO and CO₂、H₂、CH₄And the content is less than 5mg/Nm³Particulate matter of (2) and trace amounts of tar and H₂S、NH₃And water vapor without conversion. The synthesis gas is washed by water to become semi-water gas needed by the process for standby.

4) After the self-cleaning filter 17 is added, the washing circulating water only contains trace particles, organic matters and water-soluble gas and almost does not contain salt, the quality of the washing water is close to the level of soft water, and the washing water is introduced into a jacket of the normal-low pressure gasification device 11 and a heat exchanger 13 to be changed into water vapor which is used as a gasification agent and is 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 to cause serious atmospheric pollution.

In the new process, the washing water is cooled by the water heat exchanger 18, the circulation process is completely closed, any volatile gas and aerosol cannot be discharged to the atmosphere, and meanwhile, the contents of dust, oil gel and the like in the washing water are low, so that pipeline blockage and heat exchanger blockage cannot be caused.

6) Recycling water granulated slag and dry slag, namely discharging ash generated by an 11-normal-low pressure gasification device, a 12-primary-effect gas-solid separation device and a 13-heat exchanger and 17-self-cleaning type filtering and trapping dry ash (carbon-containing ash, aerosol, tar, salt and the like) to a specified area through conveying equipment, wherein the discharged ash generally contains fixed carbon and tar components (the calorific value is 3000 kilocalories/kilogram), and can be generally returned to a boiler section for mixed combustion to generate steam, and fly ash is converted into boiler fly ash through combustion for comprehensive utilization; thereby avoiding a large amount of water slag in the waste water which is washed by the original water and the washing tower.

The above are only the basic implementation methods given by the applicant according to the technical scheme and do not represent all the invention; any technical equivalent technical solutions that are not substantial improvements made by those skilled in the art according to the present disclosure should be considered to fall within the scope of the present invention.

Claims

The self-cleaning filter is characterized by comprising a reverse pressurizing ash removal area (171), a dry dedusting and desalting area (172), a pressure atomization area (173) and an ash storage and discharge area (174), wherein the reverse pressurizing ash removal area (171) enables dust, glue and salt adsorbed outside the filter bags to vibrate and shake off by rotating a double-arm reverse pressurizing gas back-blowing filter bag, the dry dedusting and desalting area (172) physically filters the dust, glue and salt in the gas through the filter bags and the filter membranes which are arranged in the circumferential direction, the pressure atomization area (173) adjusts the temperature and catches the aerosol through atomizing medicaments and water so as to promote and realize aerosol droplet growth and is matched with physical filtration to remove the glue and tar, the ash storage and discharge area (174) is used for storing the ash, the glue and the salt and controlling the ash discharge, the glue and the salt, and the pressure atomization area is preferably a pressure atomization semi-dry tar removal area.
2. A self-cleaning filter according to claim 1, wherein the ash storage and removal region (174) is conical, the ash storage and removal region (174) being connected to the self-cleaning filter cartridge; a nitrogen cannon (1744) is arranged on the side wall of the cone of the ash storage and discharge area (174), and a loading level indicator (1741), a storage temperature measuring device (1742) and a discharging level indicator (1743) are arranged on the side wall of the cone opposite to the nitrogen cannon (1744) from top to bottom.
3. A self-cleaning filter as claimed in claim 2, wherein the lower valve is opened to discharge ash when the stored ash layer is sensed to reach the loading level, the lower valve is closed to continue storing ash when the stored ash layer is sensed to reach the unloading level, and the nitrogen cannon (1744) provided on the side wall of the cone shakes off the ash accumulated on the side wall of the cone by means of the vibration caused by the instantaneous release of the pulsed high-speed released nitrogen.
4. A self-cleaning filter according to claim 2, characterised in that the level indicator (1741) is adapted to monitor an upper limit for ash storage, the level indicator (1741) being adapted to provide an ash discharge activation signal to the self-cleaning filter in the form of a digital display or a vibration signal or an audible alarm when ash storage is detected as reaching the upper limit for the high level.
5. The self-cleaning filter of claim 1, wherein the dry dedusting and desalting area is dedusted by a cloth bag to complete dedusting and desalting, the mouth of the filter bag (21) is fixedly connected to the circular mouth of the faceplate (22), the faceplate (22) is provided with a plurality of circular mouths, and each circular mouths are tightly connected with filter bags (21).
6. The self-cleaning filter of claim 1, wherein the filter bags are circumferentially distributed around the self-cleaning filter cylinder as a center, the filter bags comprise a support frame and a filter bag outer bag, the cross sections of the support frame and the filter bag outer bag are both in an ellipse-like shape 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 size of the support frame is matched with that of the filter bag outer bag.
7. A self-cleaning filter according to claim 1, wherein the reverse pressurised soot cleaning zone (171) comprises a reverse dosing soot cleaning zone comprising a nozzle (1711), a rotary blowing arm (1712), a rotary blowing tube (1713), a sealing portion (1714), a motor and gear transmission (1715), a blowing drum (1716), a pulse valve (1717); the nozzle (1711) is disposed along the rotary blowing arm (1712).
8. A self-cleaning filter according to claim 1, wherein the reverse pressure ash removal zone (171) employs a rotary double arm reverse pressure ash removal and is organically combined with the dry dust removal salt removal zone (172).
9. A self-cleaning filter according to claim 1 or 2, characterised in that the pressure atomisation region (173) comprises a dosing tank (1731), a dosing pump (1732), a temperature control system (1733) and an atomising spray head (1734), the dosing tank (1731) being connected to the atomising spray head (1734) in turn via the dosing pump (1732) and the temperature control system (1733).
10. Self-cleaning filter according to claim 1 or 2, characterised in that in the pressure atomisation zone the medicament stored in the dosing tank (1731) is dosed by means of a dosing pump (1732) and an atomising spray head (1734) at an atomisation pressure of between 3 and 4bar and the flow of the dosed spray is controlled by means of a temperature control system (1733).
11. A self-cleaning filter according to claim 1 or 2, wherein the pressure atomizing area (173) further comprises a gas distribution plate (1735), the gas distribution plate (1735) is arranged at the lower part of the atomizing nozzle, and the atomizing nozzle (1734) is arranged at the upper part of the gas distribution plate and the lower part of the filter bag (21).
12. Self-cleaning filter according to claim 1 or 2, characterised in that the counter-pressurized ash removal zone (171), the dry dedusting salt removal zone (172), the pressure atomisation zone (173) and the ash storage and discharge zone (174) are integrated in conical vessels, the counter-pressurized ash removal zone (171) being the uppermost and the dry dedusting salt removal zone (172) being the next lower part, the pressure atomisation zone (173) being the middle and the ash storage and discharge zone (174) being the lowest.
13. A self-cleaning filter according to claim 1 or 2, wherein the reverse pressurised soot cleaning zone (171) is geared with a multi-stage motor such that the rotational speed of the rotating double or multiple arms is less than 5 revolutions per minute.
14, kinds of coal gas many pollution sources ization treatment system, it includes normal low pressure gasification equipment (11), primary effect gas-solid separator (12), heat exchanger (13), scrubber tower (14), self-cleaning filter (17) and water heat exchanger (18), characterized by that, normal low pressure gasification equipment (11), primary effect gas-solid separator (12), heat exchanger (13), self-cleaning filter (17), scrubber tower (14) and water heat exchanger (18) connect gradually, and primary effect gas-solid separator (12) as the subsequent treatment device of normal low pressure gasification equipment (11), heat exchanger (13) as the subsequent treatment device of primary effect gas-solid separator (12), filter (17) as the subsequent treatment device of heat exchanger (13), scrubber tower (14) as the subsequent treatment device of self-cleaning filter (17), water heat exchanger (18) as the subsequent treatment device of scrubber tower (14).
15. The coal gas multi-pollution source gasification treatment system according to claim 14, wherein the raw gas is discharged from a normal-low pressure gasification device (11), after large particle materials are removed by a primary gas-solid separation device (12), the raw gas enters a heat exchanger (13) for waste heat recovery, the raw gas after heat exchange enters a self-cleaning filter (17) to become clean gas, and then enters a gas scrubber (14) for to cool the gas, and the clean gas enters a back-end process.
16, normal and low pressure coal gas multi-pollution source integrated treatment system, which comprises four processes of normal pressure gasification, cyclone separation, waste heat recovery, washing separation and cooling recovery, and is characterized in that sets of washing separation process composed of self-cleaning filter (17) and ash bin (45) and cooling recovery process composed of direct cooling tower (46) and cooling tower (48) respectively connected with waste heat boiler (43) and self-cleaning filter (17) after the waste heat recovery process, thereby forming normal and low pressure coal gas multi-pollution source integrated treatment system without pollution leakage.
17. The kinds of normal and low pressure coal gas multi-pollution source integrated treatment system as claimed in claim 16, wherein an inlet of the self-cleaning filter (17) is connected to a hot gas outlet of the waste heat boiler (43) to obtain a high temperature source of waste heat cooled by the waste heat boiler, an outlet at the upper part of the self-cleaning filter (17) is connected to a direct cooling tower (46) in a cooling and recycling process, an outlet at the lower part of the self-cleaning filter (17) is connected to an ash bin (45) through a conveyor (49) to convey waste in a self-cleaning process, and the ash bin (45) discharges accumulated ash through a conveying pipeline to the outside of the ash generated in an upstream process.