CN211471320U

CN211471320U - Normal and low pressure coal gas making system and multi-pollution source integrated treatment system thereof

Info

Publication number: CN211471320U
Application number: CN201921582292.9U
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: 2020-09-11
Anticipated expiration: 2029-09-23
Also published as: CN210595945U; CN110129096B; CN110129097A; CN210134067U; CN110129096A; CN110129097B; CN211546442U

Abstract

The utility model provides a normal and low pressure coal gas system and many pollution sources integration treatment system thereof, normal and low pressure coal gas system uses self-cleaning filter, and self-cleaning filter for normal and low pressure coal gas system includes reverse pressurization deashing district, dry process dust removal desalination district, pressure atomization district and ash storage deashing district, and reverse pressurization deashing district is through rotatory double-armed reverse pressurization gas blowback filter bag for dust, glue, salt vibration and shake that adsorb outside the filter bag and fall; the dry dedusting and desalting area is provided with a filter bag and a filter membrane in the circumferential direction to physically filter dust, glue and salt in the gas; the pressure atomization area adjusts the temperature and catches the aerosol through atomized medicament and water, promotes and realizes the growth of aerosol droplets, and is matched with physical filtering 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.

Description

Normal and low pressure coal gas making system and multi-pollution source integrated treatment system thereof

Technical Field

The utility model belongs to the technical field of the industry coal gas technology and specifically relates to a normal low pressure coal gas system and many pollution sources integration treatment system thereof, it is applicable to the high efficiency and filters substances such as dirt, glue, salt among the normal low pressure coal gas system. The normal-low pressure coal gas making system uses a self-cleaning filter.

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 gas composition: under the combined action of oxygen (air, oxygen-enriched oxygen and pure oxygen) and steam, the carbon in the raw material coal is incompletely combusted in a certain temperature range to generate raw coke oven gas,

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.

SUMMERY OF THE UTILITY MODEL

Based on the problem among the prior art, the utility model provides a normal low pressure coal gas system and many pollution sources integration treatment system thereof, it is applicable to the high efficiency and filters substances such as dirt, glue, salt among the normal low pressure coal gas system.

According to the first technical scheme of the utility model, a normal and low pressure coal gas making system is provided, which comprises a reverse pressurizing ash cleaning area, a dry dedusting and desalting area, a pressure atomization area and an ash storage and discharging area, wherein the reverse pressurizing ash cleaning area reversely pressurizes gas to reversely blow a filter bag through rotating a double arm, so that dust, glue and salt adsorbed outside the filter bag vibrate and shake off; the dry dedusting and desalting area physically filters dust, glue and salt in the gas through a filter bag and a filter membrane which are arranged annularly; the pressure atomization area adjusts the temperature and catches the aerosol through an atomization medicament and water so as to promote and realize the growth of aerosol droplets, and the physical filtration is matched 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 process tar removal zone.

The ash storage and discharge area is in a cone shape and is connected with the self-cleaning filter cylinder; the side wall of the cone of the ash storage and discharge area is provided with a nitrogen cannon, and the side wall of the cone opposite to the nitrogen cannon is preferably provided with a feeding level indicator, a storage temperature measuring device and a discharging level indicator from top to bottom. The material loading level indicator is used for monitoring the upper limit of stored ash, and when the stored ash is detected to reach the upper limit of a high material level, the material loading level indicator can send an ash discharge starting signal to the self-cleaning filter in the forms of digital display, vibration signals or sound alarms and the like. When the stored ash layer is detected to reach the loading level, opening a lower valve to discharge ash; and when the stored ash layer is detected to reach the material discharging position, closing the lower valve and continuously storing the ash. The nitrogen cannon arranged on the side wall of the cone of the ash storage and discharge area shakes off the dust gathered on the side wall of the cone by means of the vibration generated by the instantaneous release of the nitrogen released at high speed by the pulse. And the dry dust removal area removes dust through a cloth bag to finish dust removal and desalination. The mouth part of the filter bag is fixedly connected to the circular mouth of the card, a plurality of circular mouths are arranged on the card, and each circular mouth is tightly connected with a filter bag. When the high-speed airflow passes through the filter bag, the dust and the glue salt are filtered.

The normal-low pressure coal gas making system takes a self-cleaning filter cylinder body as a central ring to distribute filter bags, each filter bag comprises a support frame and a filter bag outer bag, the cross sections of the support frame and the filter bag outer bags are oval-like or other shapes, the support frame is arranged in the filter bag outer bags in the interior and used for supporting the filter bag outer bags, and the support frame and the filter bag outer bags are matched 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 nozzle is arranged along the rotary blowing arm. The reverse pressurizing ash removal area adopts the characteristics of rotating double-arm reverse pressurizing ash removal and is organically combined with the dry method dedusting and desalting area, so that the ash removal effect which uses the minimum capacity to reach the maximum can be achieved. The pressure atomization area comprises a dosing tank, a dosing pump, a temperature control system and an atomization nozzle, and the dosing tank is connected with the atomization nozzle through the dosing pump and the temperature control system in sequence. In the pressure atomization area, the medicine stored in the medicine adding box is added with medicine and atomized by a medicine adding pump and an atomization nozzle, the atomization pressure is generally between 3bar and 4bar, and the flow of the medicine adding spray is controlled by a temperature control system.

Preferably, the pressure atomization zone further comprises a gas distribution plate which is arranged at the lower part of the atomization nozzle; the atomizing nozzles are arranged on the upper part of the gas distribution plate and the lower part of 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 a conical container; the top part is a reverse pressurizing ash cleaning area, and the next lower part is a dry dedusting and desalting area; the lower part is a pressure atomization area, and the last part is an ash storage and discharge area. The reverse pressurizing ash removing area adopts multi-stage motor gear transmission, so that the rotating speed of the rotating double arm or the rotating multi-arm is less than 5 revolutions per minute.

The second technical scheme of the utility model, the utility model provides a many pollution sources of coal gas integration treatment system, it is including normal low pressure gasification equipment, just imitate gas-solid separator, a heat exchanger, the scrubber, self-cleaning filter and water heat exchanger, normal low pressure gasification equipment, just imitate gas-solid separator, a heat exchanger, self-cleaning filter, scrubber and water heat exchanger pressure atomization district connects gradually, and just imitate gas-solid separator pressure atomization district as normal low pressure gasification equipment's subsequent processing apparatus, heat exchanger is as the subsequent processing apparatus who just imitates gas-solid separator pressure atomization district, self-cleaning filter is as heat exchanger's subsequent processing apparatus, the scrubber is as self-cleaning filter's subsequent processing apparatus, water heat exchanger is as the subsequent processing apparatus of scrubber.

In the coal gas multi-pollution source integrated treatment system, crude 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 zone of a primary-effect gas-solid separation device; the crude gas after heat exchange enters a self-cleaning filter to be changed into clean gas, and then enters a gas washing tower to further cool the gas, and then enters a back-end process. The gas enters a gas washing tower to be cooled and then becomes clean coal gas with the temperature lower than 50 ℃. Preferably, the normal-low pressure gasification device is used for gasifying lump coal and coal powder to form crude coal 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 or laterally below the first inlet; the gasification agent steam inlet is also arranged on the side surface of the tank body and penetrates through the jacket to enter the tank body; an incremental washing water inlet and a jacket steam outlet are respectively arranged at the outer side of the jacket; the first inlet penetrates through the jacket to enter the storage tank body and is used for feeding the lump coal and the pulverized coal into the storage tank body.

In the coal 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 atomization area at the middle lower part and a reverse pressurizing ash removal area at the upper part, wherein the ash storage area is used for storing filtered dust, and the dust is accumulated to a certain material level and then is discharged downwards through a dry residue outlet; the top of the pressure atomization area is provided with an atomization nozzle, the outer side of the pressure atomization area is provided with a dosing tank, a dosing pump and a temperature control system, 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 scrubber tower is used for washing and cooling the clean coal gas to below 50 ℃ by using washing 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 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; an atomization device is arranged in the main tank body of the gas washing tower and is connected with a washing water inlet for atomizing the washing water.

The third technical scheme of the utility model, a many pollution sources of normal low pressure coal gasification integration treatment system is provided, it includes four big processes of ordinary pressure gasification, cyclone separation, waste heat recovery, washing separation and cooling recovery: after the waste heat recovery process, a set of washing and separating process consisting of a self-cleaning filter and an ash bin and a set of waste heat boiler are newly arranged.

Preferably, an inlet of the self-cleaning filter is connected with a hot air outlet of the waste heat boiler to obtain a waste heat high-temperature air source 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 a conveyor to realize the conveying of waste in a self-cleaning process, and the ash bin discharges accumulated ash together with ash generated in an upstream process through a conveying pipeline. Further, self-cleaning filter include casing, sensing detection control unit, pressure atomization unit, import cut off valve subassembly, export cut off valve subassembly backwash unit and filter unit, filter unit set up the well upper portion at self-cleaning filter, play the filtering action from bottom to top.

Compared with the prior art, compared with the prior bag-type dust remover which generally adopts the pulse back blowing of inert gas, the gas quantity (standard dry) of one group is 45000Nm³The cloth bag dust remover for coal gas production usually is in 4 single tanks and above, the utility model discloses a rotatory double-arm reverse pressurization recoil deashing technique combines high-efficient nozzle, and single tank treatment (mark is dry) tolerance can reach 45000Nm³The utility model discloses overall structure is compacter to a large amount of reductions move parts and instrument configuration.

For 45000Nm³The pulse valves adopted by the utility model are 1-2, and the total number of nozzles is greatly reduced to 20-30; while the existing line blowing needs to be equipped with a pulse valve for each line, 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 single-tank crude gas treatment capacity of the utility model can reach 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 for a normal and low pressure coal gas production system according to 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 and salt in the normal and low pressure coal gas making 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 coal gas system at both low and high pressures;

FIG. 19 is a schematic view of the integrated treatment process for multiple pollution sources in coal gas production according to 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 first 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 view of a second coal-to-gas multi-pollution-source integrated abatement process according to the present invention;

FIG. 27 is a schematic view of a third coal gas multi-pollution-source integrated treatment process according to 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 using a two-stage scrubber process.

FIG. 30 is a schematic view of a fourth embodiment of the integrated treatment system for multiple pollution sources in coal gas according to 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 explained and the embodiment of the invention is given below by combining the attached drawings of the specification.

The utility model provides a self-cleaning formula filter can be applied to normal low pressure coal gas system, and its main action lies in: the method is characterized in that particles, salt and coal tar in the raw gas are removed by physical filtration, solid particles can be removed by a clean filter at a rate of more than or equal to 99.99%, and the removal rate of the tar is more than or equal to 90%. 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 atomization area 173, the reverse pressurization ash cleaning area 171 and the ash storage and discharge area 174 are organically combined into a whole, so that 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, the tar removal technology of the pressure atomization semi-dry method is utilized in the pressure atomization area 173, so that the dosing tank 31, the dosing pump 1732, the temperature control system 1733, the atomization nozzle 1734 and the gas distribution plate are organically combined, the automatic control of the temperature of the flue gas is realized, and the atomization liquid is configured for control, so that the removal rate of micron and submicron aerosol and tar in the flue gas reaches more than 90%.

The following describes the self-cleaning filter for the normal and low pressure coal gas making system in detail with reference to the attached drawings.

As shown in fig. 3, the self-cleaning filter for the normal and low pressure coal gas making system comprises a reverse pressurizing ash cleaning area 171, a dry dedusting and desalting area 172, a pressure atomizing area 173 and an ash storage and discharge area 174, wherein the reverse pressurizing ash cleaning area 171 reversely blows the filter bag by rotating the double-arm reverse pressurizing gas, so that the dust colloid 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 structural view of the ash storage and discharge area 174 of fig. 3, wherein the ash storage and discharge area 174 has a cone shape, and the cone-shaped ash storage and discharge area is connected with a self-cleaning filter cylinder and is used for storing ash (containing tar and salt) and discharging ash; when the stored ash layer is detected to reach the loading level, opening a lower valve to discharge ash; and when the stored ash layer is detected to reach the material discharging position, closing the lower valve and continuously storing the ash. The nitrogen cannon 1744 arranged on the side wall of the cone of the ash storage and discharge area shakes off the dust gathered on the side wall of the cone by means of the vibration generated by the instantaneous release of the nitrogen released at high speed by pulse. A nitrogen cannon 1744 is arranged on one side wall of the cone, and a material loading level meter 1741, a storage temperature measuring device 1742 and a material unloading level meter 1743 are preferably arranged on the side wall of the cone opposite to the nitrogen cannon 1744 from top to bottom; in addition, a charging level meter 1741, a storage temperature measuring device 1742, and a 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, and 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 to an atomizer 1734 via a dosing pump 1732 and a temperature control system 1733 in sequence. In the pressure atomization area, the medicine stored in the medicine adding tank 1731 is added with medicine and atomized by a medicine adding pump 1732 and an atomization nozzle 1734, the atomization pressure is generally 3bar to 4bar, and the flow rate of the medicine adding spray is controlled by a temperature control system 1733. The temperature of the atomized medicament is controlled to capture aerosols and tars. The pressure atomizing area 173 further includes a gas distribution plate 1735, the gas distribution plate 1735 is disposed at the lower portion of the atomizing nozzle for cutting the whole gas flow into small gas flows to prevent the turbulence of the gas flow; the atomizing nozzles 1734 are arranged on the upper part of the gas distribution plate and the lower part of the filter bag 21, and mainly have the functions of atomizing the medicament and capturing aerosol and tar. The atomizer 1734 is preferably a pressure atomizer.

Fig. 7 is a schematic diagram of an arrangement structure of the pressure atomizing nozzle 1734 in fig. 6. In the pressure atomization area 173 of the self-cleaning filter, the pressure atomization nozzles are uniformly distributed on the half circumference of the shell on one side of the self-cleaning filter, and are installed in the cylinder of the self-cleaning filter through connecting flange pipelines, so that the aim of uniform atomization is mainly achieved, the atomization radius is large, and the aim of fully capturing aerosol and tar is fulfilled. In the utility model, 7 pressure atomizing nozzles 1734 (pressure atomizing nozzles connected with an H port) arranged in parallel are preferred, and the spraying directions of the pressure atomizing nozzles 1734 arranged in parallel are all shot into the self-cleaning filter cylinder in parallel; two large-diameter spray heads (M-port connected pressure atomizer) are preferably arranged along the radius direction of the self-cleaning filter cartridge on opposite sides of 7 pressure atomizer 1734 arranged in parallel. The pressure atomizing nozzles are connected through pressure atomizing nozzle connecting pipelines. The two M-port pressure atomizing nozzle connecting pipelines are arranged at right angles and form a triangular symmetrical relation with the H-port pressure atomizing nozzle connecting pipeline arranged in the middle.

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, wherein the dry dedusting and desalting zone completes dedusting and desalting through cloth bag dedusting. The mouth of the filter bag 21 is fixedly connected to the circular mouth of the card 22, a plurality of circular mouths are arranged on the card 22, and each circular mouth is tightly connected with one filter bag 21. When the airflow passes through the filter bag, the dust and the glue salt are filtered.

Fig. 10 is a connection structure of the cloth bag shown in fig. 9 and the card, and fig. 11 is a schematic arrangement diagram of the cloth bag shown in fig. 9, which changes the distribution of the original filter bags by blowing (fig. 1) by distributing the filter bags in a circular direction, so that the distribution of the filter bags is more compact, more filter bags are arranged in a unit area, and the filtering efficiency is higher than 40%. The filter bag includes support frame and filter bag outer bag, the cross section of support frame and filter bag outer bag is class ellipse circular or other shapes, places the filter bag outer bag in the support frame in for prop up the filter bag outer bag, support frame and filter bag outer bag size looks adaptation. The ellipse-like shape is an ellipse shape and a runway shape containing a straight section. The support frame main body is a rigid cage frame, and the support frame comprises a support opening section, a through section and a tail end section which are directly and rigidly connected in sequence; the support mouth section is hollow concentric elliptical ring structure, the cross section of the support mouth section is inverted 'concave', the inner concentric ring layer and the outer concentric ring layer are respectively connected with the upper mouth section through a sealing layer in a closed mode, the inner concentric ring layer (keel inner ring), the outer concentric ring layer (keel outer ring) and the sealing layer form a hollow area, and the hollow area is adaptive to the opening end of the outer bag of the filter bag. The straight section of the support frame comprises a straight radial rigid support keel and a transverse rigid support keel, and the transverse rigid support keel is fixed around the outer periphery or the inner periphery of the straight radial rigid support keel. The tail end section of the support frame is of an inverted cone-shaped structure, the tail end section of the support frame is composed of rigid support keels, and the rigid support keels comprise upper keels, bottom keels and middle through keels, and the upper keels and the bottom keels are fixedly connected together through the middle through keels. The support frame inside the filter bag is used for supporting the filter bag, preventing the filter bag from collapsing, and simultaneously facilitating the removal and redistribution of dust cakes.

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.

Further, as shown in fig. 10-11, the card is clamped in a groove (clamping structure, i.e. bag ring) of the outer bag of the filter bag, and the card is fixed under the clamping of the groove, and the card is used for integrally fixing the filter bag. At the moment, the outer layer of the filter bag outer bag is in contact with the pattern plate, and the inner layer of the filter bag outer bag is in contact with the support frame. Application scenarios: the dust removal box body is divided into an upper layer and a lower layer by the pattern plate, the upper layer of the pattern plate is a clean room, the lower layer of the pattern plate is a dust removal recovery room, and the assembled filter bag is positioned in the dust removal recovery room; the card is provided with an opening, and the filter bag is vertically arranged at the opening.

The installation process of the filter bag and the pattern plate is as follows: the outer bag of the filter bag is lightly inserted into the hole of the pattern plate, the opening of the outer bag of the filter bag is firmly grasped, and the outer bag of the filter bag is slowly fed into the pattern plate until the body of the outer bag of the filter bag is naturally vertical; the groove-shaped spring ring (groove (clamping structure, namely bag ring)) of the outer bag of the filter bag is tightly held by two hands, the buckling spring ring is in a C shape, one side of the embedded C-shaped spring ring is held by one hand, and the other side of the C-shaped spring ring is fixed on the edge of the pattern plate in a raised C shape; slowly, the other side of the spring ring of the outer bag of the filter bag is stretched and opened, and the groove of the spring ring is just embedded into the inner side of the plate hole. After the filter bag outer bag is installed, the filter bag support frame is slowly placed into the filter bag outer bag, and the filter bag support frame is forbidden to fall freely, so that 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 embedded and sleeved on the opening of the filter bag outer bag.

Furthermore, the filter bag is fixedly connected with the tower top base through the cleaning chamber, and the pattern plate is installed on the tower top base. The clean room is usually fixedly connected to a fixed beam at the top of the urea prilling tower, and the other end of the clean room is hermetically welded with the dust remover box body. The filter bag is fixedly positioned with the dust removal box body through the pattern plate, the pattern plate divides the dust removal 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 recovery chamber; the card 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 removal box body is provided with an opening, and the upper edge of the dust removal box body is arranged on the clean room. Still be equipped with the draught fan on the clean room, the draught fan includes air inlet and gas vent, the air inlet of draught fan passes through the pipeline and is connected with the clean room. During dust removal operation, the draught fan constantly takes the air in the clean room above the dust removal box body out, consequently forms the air current of upflow in urea prilling tower, and the air current is mingled with the dust particulate matter and is washed towards the filter bag, and the dust particulate is adsorbed by the filter bag, and clean air passes through the filter bag and gets into the clean room from the trompil department of card, and the gas vent via the draught fan is discharged. The sonic ash cleaner is preferably mounted on a rigid drum wall or beam of the urea prilling tower.

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 to a blowing drum 1716 via 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 view of the motor and gear assembly of FIG. 12; the motor 154 drives the bevel gear pair 153, the bevel gear pair 153 engages with the pinion 152, and the pinion 152 engages with the bull gear 151 to achieve the required rotational speed of the rotary blowing arm 1712, which is generally less than 5 rpm.

Fig. 16 is a flow chart of a self-cleaning filter using the present invention, which includes the following steps:

firstly, cutting crude 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 and salt in the normal and low pressure coal gas making system using the self-cleaning filter of the present invention; which comprises the following steps:

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

Into a small air flow

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 diagram of the application of the self-cleaning filter of the present invention to a coal gas system at both low and high pressures. At waste heat boiler 43 back and direct cooling tower 46 front-mounted the utility model discloses a self-cleaning filter 17 filters the ash content in the raw gas, aerosol and tar through self-cleaning filter, and wherein the clearance of ash content reaches 99.99%, and the clearance of aerosol and tar reaches 90%. The removed ash, aerosol and gum oil are transported to an ash silo. Thereby purifying the crude gas. Specifically, as shown in fig. 18, a branch line 57 directly connected to the atmospheric gasification furnace 41 is provided in the main line of the cooling tower 48 communicating with the waste heat boiler 43, and an evaporator 58 is further provided in the branch line, so that the incremental water containing oxygen, salt and oil removed from the cooling tower 48 is evaporated and fed to the atmospheric gasification furnace 1. The process flow of the multi-pollution source integrated treatment 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; 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 step A, B is performed, two output interfaces H, I and one input interface J are arranged on the lower furnace body of the waste heat boiler 43, 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. 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, a branch pipeline 57 directly connected to the normal pressure gasification furnace 41 is arranged on a main pipeline communicated to the waste heat boiler 43 through the cooling tower 48, an evaporator 58 is additionally arranged in the branch pipeline, and the incremental water which is output by the cooling tower 48 and contains the oxygen, salt and oil glue removed is sent to the normal pressure gasification furnace 41 after being subjected to evaporation treatment; therefore, under the condition 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 is sent into the normal pressure gasification furnace 41 to participate in the gasification of the lump coal.

Furthermore, the basis the utility model provides an additional technical scheme, the utility model provides a many pollution sources of coal gas integration treatment system and method, as shown in fig. 19, many pollution sources of coal gas integration treatment system includes normal low pressure gasification equipment 11, just imitates gas-solid separator 12, heat exchanger 13, scrubbing tower 14, self-cleaning formula filter 17, water heat exchanger 18. The crude gas is discharged from a normal-low pressure gasification device 11, large particle materials are removed by a primary gas-solid separation device 12, then the crude gas enters a heat exchanger 13 for waste heat recovery, the crude gas after heat exchange enters a self-cleaning filter 17 to become clean gas, then the clean gas enters a gas washing tower 14 for further cooling the gas to become clean gas with the temperature lower than 50 ℃, and the clean gas enters a back-stage process; the washing water is cooled by the water heat exchanger 18 and then returned to the scrubber 14 for recycling. One part of the incremental washing water is recycled to 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 the incremental washing water is changed into steam to be recycled to the normal-low pressure gasification device 11 through the heat exchanger 13; 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.

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 apparatus 11 is used for gasifying lump coal, pulverized coal and the like into raw coal gas, and includes a tank body, a jacket coaxial with the tank body is arranged outside the tank body, a first inlet 113 is arranged on a side surface (preferably arranged at the middle upper part) of the tank body, a second inlet 114 is arranged on a side surface (preferably arranged at the middle lower part) of the tank body, and the second inlet 114 is positioned below or laterally below the first inlet 113; a gasifying agent steam 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 wash water inlet 117 and a jacket steam outlet 115 are provided on the outside of the jacket, respectively. The first inlet 113 penetrates the jacket into the storage tank for feeding lump coal/pulverized coal and the like into the storage tank.

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 enters through a second inlet 114, water vapor enters from a water vapor inlet 112 of a gasification agent, and is gasified under the action of the gasification agent to form crude coal gas which is discharged from a crude coal gas outlet 111 at the top, and slag is discharged from a first slag discharge outlet 116 at the bottom. Part of the incremental water from the outlet of the scrubber enters the incremental water jacket at inlet 117 and is turned into steam which is discharged for reuse at 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 (preferably a pressure atomization semi-dry tar removing area) 173 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, and the dust is discharged downwards through a dry slag outlet 17c after being deposited to a certain level; an atomizing spray head 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 spray head 1734, the pressure atomizing area 173 is used for removing tar and aerosol, the temperature of the flue gas is locally controlled within a certain temperature range suitable for trapping the aerosol by proportion adjustment, and meanwhile, a sufficient amount of fine suspended liquid drops are generated to trap the gas, the aerosol and the tar.

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

Further, the temperature of the raw gas after passing through the heat exchanger is between 140 ℃ and 240 ℃, the raw gas enters from a raw gas inlet 17A at the side part (the position close to 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 ash cleaning zone 171, and is discharged from a clean gas outlet 17B arranged near the top side surface of the reverse pressurizing ash cleaning zone 171 to become the clean gas. 99.9% of dust, 90% or more of aerosol and tar contained in the raw gas are changed into porous particles, and the particles fall into the ash storage area 174 under reverse pressurization, and are discharged from the dry slag outlet 17C.

The utility model provides a self-cleaning filter's main function lies in: the method is characterized in that particles, salt and coal tar in the raw gas are removed by physical filtration, solid particles can be removed by a clean filter at a rate of more than or equal to 99.99%, and the removal rate of the tar is more than or equal to 90%. 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 atomization area 173, the reverse pressurizing ash cleaning area 171 and the ash storage area 174 are organically combined into a whole, so that solid particles can be removed by more than or equal to 99.99%, and the tar removal rate is more than or equal to 90%; in addition, the tar removal technology of the pressure atomization semi-dry method 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 flue gas is realized, and the removal rate of micron and submicron aerosol and tar in the flue gas reaches over 90 percent by configuring atomized liquid control.

Compared with the traditional bag-type dust remover which generally adopts the pulse back blowing of inert gas, the gas quantity (standard dry) of one group is 45000Nm³The cloth bag dust remover for coal gas production usually is in 4 single tanks and above, the utility model discloses can further adopt the reverse pressurization recoil deashing technique of rotatory both arms and combine high-efficient nozzle, single tank treatment (mark is dry) tolerance can reach 45000Nm³The utility model discloses overall structure is compacter to a large amount of reductions move part and instrument configuration, and the device is more stable safety. The single-tank crude gas processing capacity of the utility model can reach 40000Nm³Per hour and above (common gas cloth bag dust removal single-tank treatment capacity general)Often 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 degrees by using washing water, so as to meet the requirements of the next process. The gas washing 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 gas washing tower, wherein the clean gas inlet 141 is arranged at the bottom of the main tank body of the gas washing tower, the clean gas outlet 142 is arranged at the top of the main tank body of the gas washing tower, the washing water inlet 143 is arranged at one side surface of the middle upper part of the main tank body of the gas washing tower, the washing water outlet 144 is arranged at the bottom of the main tank body of the gas washing tower, and the washing water outlet 144 is positioned on a horizontal plane slightly lower than the clean gas inlet 141; an atomization device is arranged in the main tank of the scrubber tower and is connected with the washing water inlet 143 for atomizing the washing water. The atomizing means is preferably a pressure atomizer.

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.

Further, as shown in fig. 26, a steam storage tank is added on the basis of the integrated treatment system for multiple pollution sources of coal gas. 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 from the inlet 113 through the coal feeding device; air, oxygen-enriched air or pure oxygen is fed from the bottom 114 through a blower from a connector, gasifying agent steam is fed from an inlet 112, raw coal 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.

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, an alternative process is provided that uses a dividing wall cooler 24A in place of the scrubber tower 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, 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 further dividing wall type cooler 24A for reducing the temperature of the gas to become clean gas with the temperature lower than 50 ℃ and enters the back-stage flow; part of the condensed water is recycled to 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 the condensed water heat exchanger 13 is changed into steam to be recycled to the normal-low pressure gasification device 11; impurities such as dry ash and slag discharged by a normal-low pressure gasification device 11, a primary gas-solid separation device 12, a heat exchanger 13 and a self-cleaning filter are transported to a boiler for secondary blending combustion.

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.

Furthermore, a two-stage gas washing tower process is adopted in the coal gas multi-pollution source integrated treatment system and method (as shown in fig. 29). The raw gas is discharged from a normal-low pressure gasification device 11, large particles 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, then the clean gas enters a first-stage gas scrubber 34B to be cooled to a temperature which is 5 ℃ higher than 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, and the other part of high-temperature washing water enters the heat exchanger 13 to be changed into steam to be recycled to the normal-low; the purified gas cooled by the first-stage scrubber tower 34B passes through the second-stage scrubber tower 34C, is cooled to a temperature required by the process, generally below 50 ℃, and then enters the subsequent process. 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.

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

Reference will now be made in detail to another embodiment of the present invention, which is illustrated in fig. 30-31, wherein fig. 30 is a schematic diagram of a fourth embodiment of a coal gas multiple pollution source integrated treatment system according to the present invention; FIG. 31 is a schematic diagram of a self-cleaning filter employed in the system shown in FIG. 30.

As shown in fig. 30 and 31, the multi-pollution-source integrated treatment system for normal-pressure and low-pressure coal gas includes four steps 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 recycling 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 recycling process; therefore, the normal and low pressure coal gas multi-pollution source integrated treatment system without pollution leakage 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 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 a conveyor 49 to realize the conveying of waste in the self-cleaning process, and the ash bin 45 discharges accumulated ash together with the ash 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, 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 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: according to the integrated treatment system for multiple pollution sources in the normal and low pressure coal gas production, a plurality of independent devices of a complete set of equipment for producing water gas form a process flow almost close to full sealing, so that sewage, ash, waste gas and the like which may appear in each process flow can be completely formed into a closed process ring; the leakage of various pollutants such as water, gas, ash and the like in the operation of the traditional normal and low pressure coal gas making equipment is completely and effectively solved. Has great positive significance for protecting production environment and even urban environment.

In summary, the system and the process of the present invention fundamentally change the components of the clean gas after being 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 is only the basic implementation method given by the applicant according to the technical scheme, and does not represent the whole of the invention; any technical personnel in the same industry who have the same technology without substantial improvement according to the technical scheme should be regarded as belonging to the protection scope of the utility model.

Claims

1. The normal-low pressure coal gas making system is characterized in that the normal-low pressure coal gas making system uses a self-cleaning filter; the self-cleaning filter comprises a reverse pressurizing ash cleaning area (171), a dry dedusting and desalting area (172), a pressure atomizing area (173) and an ash storage and discharge area (174), wherein the reverse pressurizing ash cleaning area (171) reversely blows a filter bag by rotating double-arm reverse pressurizing gas; the dry dedusting and desalting area (172) is annularly provided with a filter bag and a filter membrane, dust, glue and salt in the gas are physically filtered, and the pressure atomization area (173) adjusts the temperature and catches the aerosol through atomizing medicaments and water; the ash storage and discharge area (174) is used for storing ash, glue and salt and controlling the discharge of the ash, the glue and the salt; 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.

2. The normal and low pressure coal gas making system according to claim 1, wherein the pressure atomization zone is a pressure atomization semi-dry decoking zone.

3. The normal-low pressure coal gas making system according to claim 1 or 2, characterized in that the ash storage and discharge area (174) is conical, and the ash storage and discharge area (174) is connected with a self-cleaning filter cylinder.

4. A coal gas multi-pollution source integrated treatment system comprises a normal-low pressure gasification device (11), an initial effect 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), it is characterized in that a normal-low pressure gasification device (11), a primary gas-solid separation device (12), a heat exchanger (13), a self-cleaning filter (17), a gas washing tower (14) and a water heat exchanger (18) are connected in sequence, and the primary gas-solid separation device (12) is used as a post-treatment device of the normal-low pressure gasification device (11), the heat exchanger (13) is used as a post-treatment device of the primary gas-solid separation device (12), the self-cleaning filter (17) is used as a post-treatment device of the heat exchanger (13), the gas washing tower (14) is used as a post-treatment device of the self-cleaning filter (17), and the water heat exchanger (18) is used as a post-treatment device of the gas washing tower (14).

5. The coal gas multi-pollution-source integrated treatment system according to claim 4, wherein the raw gas is discharged from the normal-low pressure gasification device (11), and enters the heat exchanger (13) for waste heat recovery after large-particle materials are removed by the 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 then enters a back-end process.

6. The coal-to-gas multi-pollution-source integrated treatment system according to claim 5, wherein the normal-low pressure gasification device (11) is used for gasifying lump coal and pulverized coal to form crude coal gas, the normal-low pressure gasification device (11) comprises a tank body, a jacket coaxial with the tank body is arranged outside the tank body, a first inlet (113) is arranged on the side surface of the tank body, a second inlet (114) is arranged on the side surface of the tank body, and the second inlet (114) is positioned below or laterally below the first inlet (113); a gasifying agent steam inlet (112) is also arranged on the side surface of the tank body and penetrates through the jacket to enter the tank body; an incremental washing water inlet (117) and a jacket steam outlet (115) are respectively arranged at the outer side of the jacket; a first inlet (113) penetrates through the jacket and enters the storage tank body, and is used for feeding lump coal and coal powder into the storage tank body.

7. The utility model provides a many pollution sources of normal low pressure coal gasification integration treatment system which includes four big processes of ordinary pressure gasification, cyclone separation, waste heat recovery, washing separation and cooling recovery, its characterized in that: a set of washing and separating process consisting of a self-cleaning filter (17) and an ash bin (45) and a cooling and recycling 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 recycling process; therefore, the normal and low pressure coal gas multi-pollution source integrated treatment system without pollution leakage is formed.

8. The multi-pollution-source integrated treatment system for the normal and low pressure coal gas according to claim 7, characterized in that: 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 straight 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 a conveyor (49) to realize the conveying of waste in the self-cleaning process, and the ash bin (45) discharges accumulated ash together with the ash generated in the upstream process through a conveying pipeline.